EP3207005B1 - Séparation d'éthylène à l'aide d'adsorption modulée en pression - Google Patents

Séparation d'éthylène à l'aide d'adsorption modulée en pression Download PDF

Info

Publication number
EP3207005B1
EP3207005B1 EP15861277.0A EP15861277A EP3207005B1 EP 3207005 B1 EP3207005 B1 EP 3207005B1 EP 15861277 A EP15861277 A EP 15861277A EP 3207005 B1 EP3207005 B1 EP 3207005B1
Authority
EP
European Patent Office
Prior art keywords
stream
hydrocarbon
gas stream
pressure
hydrocarbon adsorber
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
EP15861277.0A
Other languages
German (de)
English (en)
Other versions
EP3207005A1 (fr
EP3207005A4 (fr
Inventor
Lei Ji
Ai-Fu Chang
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Chevron Phillips Chemical Co LP
Original Assignee
Chevron Phillips Chemical Co LP
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Chevron Phillips Chemical Co LP filed Critical Chevron Phillips Chemical Co LP
Publication of EP3207005A1 publication Critical patent/EP3207005A1/fr
Publication of EP3207005A4 publication Critical patent/EP3207005A4/fr
Application granted granted Critical
Publication of EP3207005B1 publication Critical patent/EP3207005B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/2435—Loop-type reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/245—Stationary reactors without moving elements inside placed in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
    • C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F10/02—Ethene
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40086—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by using a purge gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/402—Further details for adsorption processes and devices using two beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

  • the present disclosure generally relates to the production of polyethylene. More specifically, this disclosure relates to a process for improving polyethylene production efficiency by recovering unreacted ethylene.
  • EP 0646603A1 and US 5470925 relate to processes comprising an ethylene stream which contains ethane as an impurity or a propylene stream which contains propane as an impurity which streams are contacted with a polymerization catalyst in a reactor, thereby producing a polymer product containing unreacted ethylene or propylene and the corresponding alkane.
  • WO 2013154907 relates to a process for component separation in a polymer production system, comprising separating a polymerization product stream into a gas stream and a polymer stream, distilling the gas stream into a light hydrocarbon stream, contacting the light hydrocarbon stream with an absorption solvent system, and recovering a waste gas stream from the absorption solvent system.
  • a process for component separation in a polymer production system comprising (a) separating a polymerization product stream into a gas stream and a polymer stream, (b) processing the gas stream in one or more distillation columns to yield a light hydrocarbon stream, wherein the light hydrocarbon stream comprises ethylene and ethane, (c) contacting at least a portion of the light hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein at least a portion of the ethane is selectively adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed ethane, and wherein the non-adsorbed gas stream comprises recovered ethylene, wherein the recovered ethylene comprises at least a portion of the ethylene of the light hydrocarbon stream, wherein the hydrocarbon adsorber comprises a zeolitic imidazolate framework (ZIF), (d) contacting at least a
  • Also disclosed herein is a process for component separation in a polymer production system, the process comprising (a) separating a polymerization product stream into a gas stream and a polymer stream, (b) processing the gas stream in one or more distillation columns to yield a light hydrocarbon stream, wherein the light hydrocarbon stream comprises ethylene and ethane, (c) contacting at least a portion of the light hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein at least a portion of the ethane is selectively adsorbed by the purged hydrocarbon adsorber at a pressure of from 1,000 kPa to 2,700 kPa to yield adsorbed ethane, wherein the non-adsorbed gas stream comprises recovered ethylene, wherein the recovered ethylene comprises at least a portion of the ethylene of the light hydrocarbon stream, wherein the light hydrocarbon stream is characterized by a temperature of from -25 °C
  • a process for component separation in a polymer production system comprising (a) separating a polymerization product stream into a gas stream and a polymer stream, (b) processing the gas stream in one or more distillation columns to yield a light hydrocarbon stream, wherein the light hydrocarbon stream comprises a first hydrocarbon and a second hydrocarbon, (c) contacting at least a portion of the light hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein at least a portion of the first hydrocarbon is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed first hydrocarbon, and wherein the non-adsorbed gas stream comprises recovered second hydrocarbon, wherein the recovered second hydrocarbon comprises at least a portion of the second hydrocarbon of the light hydrocarbon stream, wherein the hydrocarbon adsorber is characterized by an adsorption selectivity of the first hydrocarbon versus the second hydrocarbon as
  • a process for hydrocarbon recovery comprising (a) providing a hydrocarbon stream comprising a first hydrocarbon and a second hydrocarbon, wherein the first hydrocarbon is a saturated hydrocarbon, and wherein the second hydrocarbon is an olefin, (b) contacting at least a portion of the hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein at least a portion of the first hydrocarbon is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed first hydrocarbon, and wherein the non-adsorbed gas stream comprises recovered second hydrocarbon, wherein the recovered second hydrocarbon comprises at least a portion of the second hydrocarbon of the hydrocarbon stream, wherein the hydrocarbon adsorber is characterized by an adsorption selectivity of the first hydrocarbon versus the second hydrocarbon as determined by volumetric adsorption at 298 K and at the first pressure of equal to or greater than 2,
  • a pressure swing adsorption system comprising at least two pressure swing adsorption units, wherein the at least two pressure swing adsorption units are operated in parallel, wherein the pressure swing adsorption unit comprises at least one hydrocarbon adsorber bed disposed therein, wherein the hydrocarbon adsorber bed comprises a hydrocarbon adsorber, wherein the hydrocarbon adsorber is contacted with a sweeping gas stream to yield a purged hydrocarbon adsorber, wherein the pressure swing adsorption unit adsorbs at a first pressure, wherein the purged hydrocarbon adsorber adsorbs a first hydrocarbon to yield a loaded hydrocarbon adsorber comprising an adsorbed first hydrocarbon and a non-adsorbed gas stream comprising a second hydrocarbon, wherein the hydrocarbon adsorber has an adsorption selectivity of the first hydrocarbon versus the second hydrocarbon as determined by volumetric adsorption at 298 K and at the first pressure of equal to or greater than 2, wherein the
  • a process for ethylene polymerization comprising (a) polymerizing ethylene in a slurry loop reactor system to obtain a polymerization product stream, (b) separating a polymerization product stream in a flash chamber into a gas stream and a polymer stream, (c) processing the gas stream in one or more distillation columns to yield a light hydrocarbon stream, wherein the light hydrocarbon stream comprises ethane and ethylene, (d) contacting at least a portion of the light hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein at least a portion of ethane is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed ethane, and wherein the non-adsorbed gas stream comprises recovered ethylene, wherein the recovered ethylene comprises at least a portion of the ethylene of the light hydrocarbon stream, wherein the hydrocarbon adsorber is
  • a process for hydrocarbon recovery comprising (a) providing a hydrocarbon stream originating from a polymerization process, wherein the hydrocarbon stream comprises a first hydrocarbon and a second hydrocarbon, wherein the first hydrocarbon is a saturated hydrocarbon, and wherein the second hydrocarbon is an olefin, (b) loading a purged hydrocarbon adsorber with at least a portion of the first hydrocarbon to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein at least a portion of the first hydrocarbon is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed first hydrocarbon, wherein the loaded hydrocarbon adsorber comprises the adsorbed first hydrocarbon, wherein the non-adsorbed gas stream comprises recovered second hydrocarbon, wherein the recovered second hydrocarbon comprises at least a portion of the second hydrocarbon of the hydrocarbon stream, wherein the hydrocarbon adsorber is characterized by an adsorption selectivity of the first hydrocarbon
  • the systems, apparatuses, and processes are generally related to the separation of a first chemical component or compound (e.g., unreacted monomer, unreacted ethylene) from a composition resulting from petrochemical production processes, for example the production of polyethylene, and comprising the first chemical component or compound and one or more other chemical components, compounds, or the like.
  • a first chemical component or compound e.g., unreacted monomer, unreacted ethylene
  • a process for component separation in a polymer production system can generally comprise the steps of (a) separating a polymerization product stream into a gas stream and a polymer stream; (b) processing the gas stream in one or more distillation columns to yield a light hydrocarbon stream, wherein the light hydrocarbon stream comprises ethylene and ethane; (c) contacting at least a portion of the light hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein at least a portion of the ethane is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed ethane, and wherein the non-adsorbed gas stream comprises recovered ethylene, wherein the recovered ethylene comprises at least a portion of the ethylene of the light hydrocarbon stream; (d) contacting at least a portion of the loaded hydrocarbon adsorber with a sweeping gas stream at a second pressure
  • a process for component separation in a polymer production system can generally comprise selectively separating a first hydrocarbon (e.g., by-product hydrocarbon, by-product ethane) from a second hydrocarbon (e.g., unreacted monomer, unreacted ethylene), wherein the first hydrocarbon and the second hydrocarbon can be recovered from a polymerization product stream.
  • a first hydrocarbon e.g., by-product hydrocarbon, by-product ethane
  • a second hydrocarbon e.g., unreacted monomer, unreacted ethylene
  • the hydrocarbons can comprise any suitable hydrocarbons compatible with the disclosed methods and materials.
  • PEP system 1000 generally comprises a slurry loop reactor system 100, a flash chamber 200, a heavy distillation column 300, a light distillation column 350, a purge column 400, a pressure swing adsorption (PSA) unit 500, and an isobutane ( i -butane) and nitrogen recovery unit (INRU) 600.
  • various system components can be in fluid communication via one or more conduits (e.g., pipes, tubing, flow lines, etc.) suitable for the conveyance of a particular stream, for example as shown in detail by the numbered streams in Figure 1A .
  • a reagents stream 110 (also referred to as a feed stream) can be communicated to the slurry loop reactor system 100.
  • a polymerization product stream 120 can be communicated from the slurry loop reactor system 100 to the flash chamber 200.
  • a gas stream 210 can be communicated from the flash chamber 200 to the heavy distillation column 300.
  • the heavy distillation column 300 can be referred to as a first distillation column.
  • a heavy distillation bottoms stream 310 can be emitted from the heavy distillation column 300, and a heavy distillation side stream 320 can be emitted from the heavy distillation column 300.
  • An intermediate hydrocarbon stream 330 can be emitted from the heavy distillation column 300 and communicated to the light distillation column 350.
  • the light distillation column 350 can be referred to as a second distillation column.
  • a light distillation side stream 370 can be emitted from the light distillation column 350.
  • a light distillation bottoms stream 360 comprising olefin-free isobutane 365 can be emitted from the light distillation column 350.
  • a light hydrocarbon stream 380 can be communicated from the light distillation column 350 to the PSA unit 500.
  • a sweeping gas stream 510 can be communicated to the PSA unit 500. At least a portion of the olefin-free isobutane 365 can be recycled 366 to the PSA unit 500, for example via the sweeping gas stream 510.
  • a recovered adsorbed gas stream 530 can be emitted from the PSA unit 500.
  • a non-adsorbed gas stream 520 can be communicated from the PSA unit 500 to the INRU 600.
  • a gas stream 610 comprising nitrogen 615 can be emitted from the INRU 600. At least a portion of the nitrogen 615 can be recycled 617 to the PSA unit 500, for example via the sweeping gas stream 510.
  • a gas stream 620 comprising isobutane and ethylene 625 can be emitted from the INRU 600. At least a portion of the isobutane and ethylene 625 can be recycled 626 to the slurry loop reactor system 100, for example via the reagents stream 110.
  • a polymer stream 220 can be communicated from the flash chamber 200 to the purge column 400.
  • a purge gas stream 410 can be communicated to the purge column 400.
  • a purged polymer stream 420 comprising a polymer 425 can be emitted from the purge column 400.
  • a spent purge gas stream 430 can be emitted from the purge column 400.
  • At least a portion of the nitrogen 615 can be recycled 616 to the purge column 400, for example via the purge gas stream 410.
  • an "olefin-free" hydrocarbon refers to a hydrocarbon (e.g., isobutane) that can be free of olefins, alternatively, substantially free of olefins, alternatively, essentially free of olefins, or alternatively, consist or consist essentially of non-olefins.
  • olefins or alkenes are unsaturated hydrocarbons containing at least one carbon-carbon double bond.
  • olefins can be present in a substantially olefin-free hydrocarbon (e.g., substantially olefin-free isobutane) in an amount of less than 10% by total weight of the olefin-free hydrocarbon, alternatively, less than 9%, alternatively, less than 8%, alternatively, less than 7%, alternatively, less than 6%, alternatively, less than 5%, alternatively, less than 4%, alternatively, less than 3%, alternatively, less than 2%, alternatively, less than 1.0%, alternatively, less than 0.5%, alternatively, less than 0.1%.
  • a substantially olefin-free hydrocarbon e.g., substantially olefin-free isobutane
  • an amount of less than 10% by total weight of the olefin-free hydrocarbon alternatively, less than 9%, alternatively, less than 8%, alternatively, less than 7%, alternatively, less than 6%, alternatively, less than 5%, alternatively, less than 4%
  • a second PEP system 1001 which has a number of system components common with PEP system 1000.
  • the second PEP system 1001 comprises one distillation column 301 (as opposed to two distillation columns 300 and 350 of PEP system 1000).
  • the gas stream 210 can be communicated from the flash chamber 200 to the distillation column 301.
  • a distillation side stream 303 can be emitted from the distillation column 301.
  • a distillation bottoms stream 302 can be emitted from the distillation column 301.
  • a light hydrocarbon stream 304 can be communicated from the distillation column 301 to the PSA unit 500.
  • a PEP process can be described with reference to one or more examples of PEP system 1000 and/or PEP system 1001. Although a given PEP process can be described with reference to one or more examples of a PEP system, such a disclosure should not be construed as so-limiting. Although the various steps of the processes disclosed herein may be disclosed or illustrated in a particular order, such should not be construed as limiting the performance of these processes to any particular order unless otherwise indicated.
  • PEP process 2000 can generally comprise (i) a step 2100 of purifying a feed stream; (ii) a step 2200 of polymerizing monomers of the purified feed stream to form a polymerization product stream; (iii) a step 2300 of separating the polymerization product stream into a polymer stream and a gas stream; (iv) a step 2400 of purging the polymer stream to produce a purged polymer stream and a spent purge gas stream; (v) a step 2500 of processing the gas stream in one or more distillation columns to produce a light hydrocarbon stream; (vi) a step 2600 of contacting the light hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream; (vii) a step 2700 of contacting the loaded hydrocarbon adsorber with a sweeping gas stream to yield a hydrocarbon adsorber and a recovered adsor
  • step 2600 of contacting the light hydrocarbon stream with a purged hydrocarbon adsorber can also be referred to as an "adsorption step;” step 2700 of contacting the loaded hydrocarbon adsorber with a sweeping gas stream can also be referred to as a "desorption step;” and step 2800 of contacting the hydrocarbon adsorber with the sweeping gas stream can also be referred to as a "purging step.”
  • a compound e.g., first hydrocarbon, ethane, etc.
  • an adsorbed compound e.g., adsorbed first hydrocarbon, adsorbed ethane, etc.
  • the adsorbed compound can be desorbed during desorption step 2700; and the hydrocarbon adsorber can be purged in purging step 2800.
  • the PEP process 2000 or a portion thereof can be implemented via the PEP system 1000 (e.g., as illustrated in Figure 1A ) and/or the PEP system 1001 (e.g., as illustrated in Figure 1B ).
  • the PEP process 2000 is a continuous process.
  • the PEP process 2000 can generally comprise the step 2100 of purifying a feed stream or a reagents stream.
  • purifying a feed stream can comprise separating unwanted compounds and elements from a feed stream comprising ethylene to form a purified feed stream.
  • Purifying a feed stream can comprise any suitable method or process, including the non-limiting examples of filtering, membrane screening, reacting with various chemicals, absorbing, adsorbing, distillation(s), or combinations thereof.
  • a feed stream 10 (e.g., reagents stream 110 in Figure 1A and/or Figure 1B ) can be communicated to a purifier 102.
  • the feed stream 10 can comprise ethylene and various other gases, such as but not limited to methane, ethane, acetylene, propane, propylene, water, nitrogen, oxygen, various other gaseous hydrocarbons having three or more carbon atoms, various contaminants, or combinations thereof.
  • the purifier 102 can comprise a device or apparatus suitable for the purification of one or more reactant gases in a feed stream comprising a plurality of potentially unwanted gaseous compounds, elements, contaminants, and the like.
  • Non-limiting examples of a suitable purifier 102 can comprise a filter, a membrane, a reactor, an absorbent, a molecular sieve, one or more distillation columns, or combinations thereof.
  • the purifier 102 can be configured to separate ethylene from a stream comprising a plurality of potentially unwanted gaseous compounds, elements, contaminants, and the like.
  • Purifying a feed stream can yield a purified feed stream 11 comprising substantially pure monomers (e.g., substantially pure ethylene).
  • the purified feed stream can comprise less than 25% by total weight of the stream, alternatively, less than 10%, alternatively, less than 1.0% of any one or more of nitrogen, oxygen, methane, ethane, propane, comonomers, or combinations thereof.
  • substantially pure ethylene refers to a fluid stream comprising at least 60% ethylene, alternatively, at least 70% ethylene, alternatively, at least 80% ethylene, alternatively, at least 90% ethylene, alternatively, at least 95% ethylene, alternatively, at least 99% ethylene by total weight of the stream, alternatively, at least 99.5% ethylene by total weight of the stream.
  • the feed stream 11 can further comprise trace amounts of ethane, for example, as from a recycled stream, as will be discussed in more detail later herein.
  • the purified feed stream can comprise a comonomer, such as unsaturated hydrocarbons having from 3 to 20 carbon atoms.
  • comonomers that can be present in the purified feed stream include alpha olefins, such as for example propylene, 1-butene, 1-pentene, 1-hexene, 3-methyl-1-butene, 4-methyl-1-pentene, 1-heptene, 1-octene, 1-nonene, 1-decene, and the like, or combinations thereof.
  • the PEP process 2000 can generally comprise the step 2200 of polymerizing monomers of the purified feed stream to form a polymerization product stream.
  • the polymerization product stream can be formed using any suitable olefin polymerization method which can be carried out using various types of polymerization reactors.
  • the terms "polymerization reactor” or “reactor” include any polymerization reactor capable of polymerizing olefin monomers or comonomers to produce homopolymers or copolymers. Such homopolymers and copolymers are referred to as resins or polymers.
  • the various types of reactors include those that can be referred to as batch, slurry, gas-phase, solution, high pressure, tubular or autoclave reactors.
  • Gas phase reactors can comprise fluidized bed reactors or staged horizontal reactors.
  • Slurry reactors can comprise vertical or horizontal loops.
  • High pressure reactors can comprise autoclave or tubular reactors.
  • Reactor types can include batch or continuous processes. Continuous processes could use intermittent or continuous product discharge.
  • Processes can also include partial or full direct recycle of unreacted monomer, unreacted comonomer, and/or diluent.
  • the reactors considered for this disclosure could be any reactors that are part of a polymerization process that can yield a vent stream containing ethylene and ethane.
  • Polymerization reactor systems of the present disclosure can comprise one type of reactor in a system or multiple reactors of the same or different type.
  • Production of polymers in multiple reactors can include several stages in at least two separate polymerization reactors interconnected by transfer stream(s), line(s), apparatus(es) (for example, a separation vessel(s)) and/or device(s) (for example, a valve or other mechanism) making it possible to transfer the polymers resulting from a first polymerization reactor into a second reactor.
  • the desired polymerization conditions in one of the reactors can be different from the operating conditions of the other reactors.
  • polymerization in multiple reactors can include the manual transfer of polymer from one reactor to subsequent reactors for continued polymerization.
  • Multiple reactor systems can include any combination including, but not limited to, multiple loop reactors, multiple gas reactors, a combination of loop and gas reactors, multiple high pressure reactors or a combination of high pressure with loop and/or gas reactors.
  • the multiple reactors can be operated in series or in parallel.
  • the polymerization reactor system can comprise at least one loop slurry reactor comprising vertical or horizontal loops.
  • Monomer, diluent, catalyst, and optionally any comonomer can be continuously fed to a loop reactor where polymerization occurs.
  • continuous processes can comprise the continuous introduction of a monomer, an optional comonomer, a catalyst, and a diluent into a polymerization reactor and the continuous removal from this reactor of a suspension comprising polymer particles and the diluent.
  • Reactor effluent can be flashed to remove the solid polymer from the liquids that comprise the diluent, monomer and/or comonomer.
  • Various technologies can be used for this separation step including but not limited to, flashing that can include any combination of heat addition and pressure reduction; separation by cyclonic action in either a cyclone or hydrocyclone; or separation by centrifugation.
  • a suitable slurry polymerization process (also known as the particle form process), is disclosed, for example, in U.S. Patent Nos. 3,248,179 ; 4,501,885 ; 5,565,175 ; 5,575,979 ; 6,239,235 ; 6,262,191 ; and 6,833,415 .
  • Suitable diluents used in slurry polymerization include, but are not limited to, the monomer, and optionally, the comonomer, being polymerized and hydrocarbons that are liquids under reaction conditions.
  • suitable diluents include, but are not limited to, hydrocarbons such as propane, cyclohexane, isobutane, n-butane, n-pentane, isopentane, neopentane, and n-hexane.
  • the polymerization reactor can comprise at least one gas phase reactor.
  • Such systems can employ a continuous recycle stream containing one or more monomers continuously cycled through a fluidized bed in the presence of the catalyst under polymerization conditions.
  • a recycle stream can be withdrawn from the fluidized bed and recycled back into the reactor.
  • polymer product can be withdrawn from the reactor and new or fresh monomer can be added to replace the polymerized monomer.
  • copolymer product can optionally be withdrawn from the reactor and new or fresh comonomer can be added to replace polymerized comonomer, polymerized monomer, or combinations thereof.
  • Such gas phase reactors can comprise a process for multi-step gas-phase polymerization of olefins, in which olefins are polymerized in the gaseous phase in at least two independent gas-phase polymerization zones while feeding a catalyst-containing polymer formed in a first polymerization zone to a second polymerization zone.
  • Gas phase reactors are disclosed in U.S. Patent Nos. 5,352,749 ; 4,588,790 ; and 5,436,304 .
  • a high pressure polymerization reactor can comprise a tubular reactor or an autoclave reactor.
  • Tubular reactors and/or autoclave reactors can have several zones where fresh monomer (optionally, comonomer), initiators, or catalysts can be added.
  • Monomer (optionally, comonomer) can be entrained in an inert gaseous stream and introduced at one zone of the reactor.
  • Initiators, catalysts, and/or catalyst components can be entrained in a gaseous stream and introduced at another zone of the reactor.
  • the gas streams can be intermixed for polymerization. Heat and pressure can be employed appropriately to obtain optimal polymerization reaction conditions.
  • the polymerization reactor can comprise a solution polymerization reactor wherein the monomer (optionally, comonomer) can be contacted with the catalyst composition by suitable stirring or other means.
  • a carrier comprising an inert organic diluent or excess monomer (optionally, comonomer) can be employed.
  • the monomer and/or optional comonomer can be brought in the vapor phase into contact with the catalytic reaction product, in the presence or absence of liquid material.
  • the polymerization zone is maintained at temperatures and pressures that will result in the formation of a solution of the polymer in a reaction medium. Agitation can be employed to obtain better temperature control and to maintain uniform polymerization mixtures throughout the polymerization zone. Adequate means are utilized for dissipating the exothermic heat of polymerization.
  • Polymerization reactors suitable for the disclosed systems and processes can further comprise any combination of at least one raw material feed system, at least one feed system for catalyst or catalyst components, and/or at least one polymer recovery system.
  • Suitable reactor systems can further comprise systems for feedstock purification, catalyst storage and preparation, extrusion, reactor cooling, polymer recovery, fractionation, recycle, storage, loadout, laboratory analysis, and process control.
  • Conditions e.g., polymerization conditions that are controlled for polymerization efficiency and to provide resin properties include temperature, pressure, type and/or quantity of catalyst or co-catalyst, and concentrations and/or partial pressures of various reactants.
  • Polymerization temperature can affect catalyst productivity, polymer molecular weight and molecular weight distribution.
  • Suitable polymerization temperature can be any temperature below the de-polymerization temperature according to the Gibbs Free energy equation. Typically this includes from 60 °C to 280 °C, for example, and from 70 °C to 110 °C, depending upon the type of polymerization reactor.
  • Suitable pressures will also vary according to the reactor and polymerization type.
  • the pressure for liquid phase polymerizations in a loop reactor is typically less than 1,000 psig.
  • Pressure for gas phase polymerization is usually at 200 psig to 500 psig.
  • High pressure polymerization in tubular or autoclave reactors is generally run at 20,000 to 75,000 psig.
  • Polymerization reactors can also be operated in a supercritical region occurring at generally higher temperatures and pressures. Operation above the critical point of a pressure/temperature diagram (supercritical phase) can offer advantages. Polymerization can occur in an environment having a suitable combination of temperature and pressure.
  • polymerization can occur at a pressure in a range of from 550 psi to 650 psi, alternatively, from 600 psi to 625 psi and a temperature in a range of from 170 °F to 230 °F, alternatively, from 195 °F to 220 °F.
  • the concentration of various reactants can be controlled to produce resins with certain physical and mechanical properties.
  • the proposed end-use product that will be formed by the resin and the method of forming that product determines the desired resin properties.
  • Mechanical properties include tensile, flexural, impact, creep, stress relaxation and hardness tests.
  • Physical properties include density, molecular weight, molecular weight distribution, melting temperature, glass transition temperature, temperature melt of crystallization, density, stereoregularity, crack growth, long chain branching and rheological parameters.
  • the concentrations and/or partial pressures of monomer, comonomer, hydrogen, co-catalyst, modifiers, and electron donors are important in producing these resin properties.
  • Comonomer can be used to control product density.
  • Hydrogen can be used to control product molecular weight.
  • Cocatalysts can be used to alkylate, scavenge poisons and control molecular weight.
  • Modifiers can be used to control product properties and electron donors affect stereoregularity, the molecular weight distribution, and/or molecular weight. In addition, the concentration of poisons is minimized because poisons impact the reactions and product properties.
  • a suitable catalyst system can comprise a catalyst and, optionally, a co-catalyst (e.g., organoaluminum compound) and/or promoter.
  • suitable catalyst systems include Ziegler Natta catalysts, Ziegler catalysts, chromium catalysts, chromium oxide catalysts, chrome-silica catalysts, chrome-titania catalysts, chromocene catalysts, metallocene catalysts, nickel catalysts, or combinations thereof.
  • Catalyst systems suitable for use in the present disclosure have been described, for example, in U.S. Patent Nos. 7,163,906 ; 7,619,047 ; 7,790,820 ; and 7,960,487 and U.S. Patent Application Publication No. 2009/0004417 .
  • the catalyst system can comprise an activator.
  • the activator can be a solid oxide activator-support, a chemically treated solid oxide, a clay mineral, a pillared clay, an exfoliated clay, an exfoliated clay gelled into another oxide matrix, a layered silicate mineral, a non-layered silicate mineral, a layered aluminosilicate mineral, a non-layered aluminosilicate mineral, an aluminoxane, a supported aluminoxane, an ionizing ionic compound, an organoboron compound, or any combination thereof.
  • the terms “chemically-treated solid oxide,” “solid oxide activator-support,” “acidic activator-support,” “activator-support,” “treated solid oxide compound,” and the like are used herein to indicate a solid, inorganic oxide of relatively high porosity, which exhibits Lewis acidic or Bronsted acidic behavior, and which has been treated with an electron-withdrawing component, typically an anion, and which is calcined.
  • the electron-withdrawing component is typically an electron-withdrawing anion source compound.
  • the chemically-treated solid oxide compound comprises the calcined contact product of at least one solid oxide compound with at least one electron-withdrawing anion source compound.
  • the chemically-treated solid oxide comprises at least one ionizing, acidic solid oxide compound.
  • support and “activator-support” are not used to imply these components are inert, and such components should not be construed as an inert component of the catalyst composition.
  • Monomers in a feed stream can be polymerized.
  • Polymerizing monomers of the purified feed stream can comprise allowing a polymerization reaction between a plurality of monomers by contacting a monomer or monomers with a catalyst system under conditions suitable for the formation of a polymer.
  • Polymerizing comonomers of the purified feed stream can comprise allowing a polymerization reaction between a plurality of comonomers by contacting a comonomer or comonomers with a catalyst system under conditions suitable for the formation of a copolymer.
  • the step 2200 of polymerizing monomers of the purified feed stream to form a polymerization product stream can be carried out using a slurry loop reactor system, such as for example a slurry loop reactor system 101 illustrated in of Figure 3 .
  • the slurry loop reactor system 101 generally comprises a purifier 102, a first reactor 104, and a second reactor 106.
  • various system components can be in fluid communication via one or more conduits (e.g., pipes, tubing, flow lines, etc.) suitable for the conveyance of a particular stream, for example as shown in detail by the numbered streams in Figure 3 .
  • a purified feed stream 11 can be communicated from the purifier 102 to one or more of the reactors (e.g., a first reactor 104, a second reactor 106). Where the slurry loop reactor system comprises two or more reactors, a mid-polymerization reactor stream 15 can be communicated from the first reactor 104 to the second reactor 106. Hydrogen can be introduced into the second reactor 106 in stream 21.
  • a polymerization product stream e.g., polymerization product stream 121 in Figure 3 , polymerization product stream 120 in Figure 1A and/or Figure 1B ) can be emitted from the first reactor 104 and/or the second reactor 106.
  • polymerizing monomers of the purified feed stream can comprise routing the purified feed stream 11 to the one or more of the polymerization reactors 104, 106.
  • Polymerizing monomers of the mid-polymerization reactor stream 15 can comprise routing the mid-polymerization reactor stream 15 to polymerization reactor(s) 106.
  • polymerizing monomers of the mid-polymerization reactor stream 15 can comprise routing the mid-polymerization reactor stream 15 from polymerization reactor(s) 104 to polymerization reactor(s) 106.
  • the polymerization reactors 104, 106 can comprise any vessel or combination of vessels suitably configured to provide an environment for a chemical reaction (e.g., a contact zone) between monomers (e.g., ethylene) and/or polymers (e.g., an "active" or growing polymer chain), and optionally comonomers and/or copolymers, in the presence of a catalyst to yield a polymer (e.g., a polyethylene polymer) and/or copolymer.
  • a chemical reaction e.g., a contact zone
  • production of polymers in multiple reactors can include at least two polymerization reactors 104, 106 interconnected by one or more devices or apparatus (e.g., valve, continuous take-off valve, and/or continuous take-off mechanism). As illustrated in Figure 3 , production of polymers in multiple reactors can include at least two polymerization reactors 104, 106 interconnected by one or more streams or lines (e.g., mid-polymerization reactor stream 15). Production of polymers in multiple reactors can include at least two polymerization reactors 104, 106 interconnected by one or more separators (e.g., flash chambers).
  • separators e.g., flash chambers
  • Polymerizing monomers can comprise introducing a suitable catalyst system into the first and/or second reactor 104, 106, respectively, so as to form a slurry.
  • a suitable catalyst system can reside in the first and/or second reactor 104, 106, respectively.
  • polymerizing monomers can comprise selectively manipulating one or more polymerization reaction conditions to yield a given polymer product, to yield a polymer product having one or more desirable properties, to achieve a desired efficiency, to achieve a desired yield, the like, or combinations thereof.
  • Polymerizing monomers of the purified feed stream 11 can comprise adjusting one or more polymerization reaction conditions.
  • Polymerizing monomers can comprise maintaining a suitable temperature, pressure, and/or partial pressure(s) during the polymerization reaction, alternatively, cycling between a series of suitable temperatures, pressures, and/or partial pressure(s) during the polymerization reaction.
  • Polymerizing monomers can comprise polymerizing comonomers in one or more of polymerization reactors 104, 106. Polymerizing monomers can comprise introducing ethylene monomer and/or a comonomer to the polymerization reactor 106.
  • Polymerizing monomers can include introducing hydrogen into one or more of reactors 104 and 106.
  • Figure 3 illustrates hydrogen can be introduced into reactor 106 through stream 21.
  • the amount of hydrogen introduced into the reactor 106 can be adjusted so as to obtain, in the diluent, a molar ratio of hydrogen to ethylene of 0.001 to 0.1. This molar ratio can be at least 0.004 in reactor 106. In some examples, this molar ratio cannot exceed 0.05.
  • the ratio of the concentration of hydrogen in the diluent in reactor 104 to the concentration of hydrogen polymerization reactor 106 can be at least 20, alternatively, at least 30, alternatively, at least 40, alternatively, not greater than 300, alternatively, not greater than 200. Suitable hydrogen concentration control methods and systems are disclosed in U.S. Patent No. 6,225,421 .
  • Polymerizing monomers can comprise circulating, flowing, cycling, mixing, agitating, or combinations thereof, the monomers (optionally, comonomers), catalyst system, and/or the slurry within and/or between the reactors 104, 106.
  • circulation can be at a velocity (e.g., slurry velocity) of from 1 m/s to 30 m/s, alternatively, from 2 m/s to 17 m/s, or alternatively, from 3 m/s to 15 m/s.
  • Polymerizing monomers can comprise configuring reactors 104, 106 to yield an unimodal resin.
  • the "modality" of a polymer resin refers to the form of its molecular weight distribution curve, i.e., the appearance of the graph of the polymer weight fraction as a function of its molecular weight.
  • the polymer weight fraction refers to the weight fraction of molecules of a given size.
  • a polymer having a molecular weight distribution curve showing a single peak can be referred to as a unimodal polymer
  • a polymer having curve showing two distinct peaks can be referred to as bimodal polymer
  • a polymer having a curve showing three distinct peaks can be referred to as trimodal polymer, etc.
  • Polymerizing monomers can comprise configuring reactors 104, 106 to yield a multimodal (e.g., a bimodal) polymer (e.g., polyethylene).
  • a multimodal polymer e.g., polyethylene
  • the resultant polymer can comprise both a relatively high molecular weight, low density (HMWLD) polyethylene polymer and a relatively low molecular weight, high density (LMWHD) polyethylene polymer.
  • HMWLD low density
  • LWHD high density
  • various types of suitable polymers can be characterized as having a various densities.
  • a Type I polymer can be characterized as having a density in a range of from 0.910 g/cm 3 to 0.925 g/cm 3
  • a Type II polymer can be characterized as having a density from 0.926 g/cm 3 to 0.940 g/cm 3
  • a Type III polymer can be characterized as having a density from 0.941 g/cm 3 to 0.959 g/cm 3
  • a Type IV polymer can be characterized as having a density of greater than 0.960 g/cm 3 .
  • polymerizing monomers of the purified feed stream 11 can yield polymerization product stream 121.
  • the polymerization product stream 121 e.g., polymerization product stream 120 in Figure 1A and/or Figure 1B
  • Polymerizing monomers of the purified feed stream 11 can yield the polymerization product stream 121 generally comprising unreacted monomer (e.g., ethylene), optional unreacted comonomer, by-products (e.g., ethane, which can be by-product ethane formed from ethylene and hydrogen), and a polymerization product (e.g., polymer and optionally, copolymer).
  • unreacted monomer e.g., ethylene
  • by-products e.g., ethane, which can be by-product ethane formed from ethylene and hydrogen
  • a polymerization product e.g., polymer and optionally, copolymer
  • an "unreacted comonomer” refers to a comonomer that was introduced into a polymerization reactor during a polymerization reaction but was not incorporated into a polymer.
  • the solids and/or liquids of the polymerization product stream 121 can comprise a polymer product (e.g., a polyethylene polymer), often referred to at this stage of the PEP process as "polymer fluff.”
  • the gases of the polymerization product stream 121 can comprise unreacted, gaseous reactant monomers or optional comonomers (e.g., unreacted ethylene monomers, unreacted comonomers), gaseous waste products, gaseous contaminants, or combinations thereof.
  • the polymerization product stream 121 can comprise hydrogen, nitrogen, methane, ethylene, ethane, propylene, propane, butane, 1-butene, isobutane, pentane, hexane, 1-hexene and heavier hydrocarbons.
  • Ethylene can be present in a range of from 0.1% to 15%, alternatively, from 1.5% to 5%, alternatively, 2% to 4% by total weight of the polymerization product stream.
  • Ethane can be present in a range of from 0.001% to 4%, alternatively, from 0.2% to 0.5% by total weight of the polymerization product stream.
  • Isobutane can be present in a range from 80% to 98%, alternatively, from 92% to 96%, alternatively, 95% by total weight of the polymerization product stream.
  • the PEP process 2000 can generally comprise the step 2300 of separating the polymerization product stream into a polymer stream and a gas stream.
  • separating the polymerization product into a polymer stream and a gas stream can generally comprise removing gases from liquids and/or solids (e.g., the polymer fluff) by any suitable process.
  • separating the polymerization product into a polymer stream and a gas stream can comprise routing the polymerization product stream 120 to a separator (e.g., flash chamber 200).
  • a separator e.g., flash chamber 200
  • tThe polymerization product stream 120 can comprise at least a portion of the polymerization product stream 121 emitted from the second reactor 106.
  • the polymerization product stream 120 can comprise at least a portion of the mid-polymerization reactor stream 15 emitted from the first reactor 104.
  • the polymerization product stream 120 can comprise at least a portion of the polymerization product stream 121 and at least a portion of the mid-polymerization reactor stream 15.
  • a separator such as flash chamber 200 can be configured to separate a stream (e.g., polymerization product stream 120 comprising polyethylene) into gases, liquids, solids, or combinations thereof.
  • a stream e.g., polymerization product stream 120 comprising polyethylene
  • the separator for separating the polymerization product stream into a polymer stream and a gas stream can comprise a vapor-liquid separator.
  • the solids of the polymerization product stream e.g., polymer fluff
  • a vapor-liquid separator would generally separate the solids and the liquid in a single slurry phase from the gases of the polymerization product stream.
  • Nonlimiting examples of separators suitable for use in the present disclosure a fixed-bed adsorption column, a flash tank, a filter, a membrane, a reactor, an absorbent, an adsorbent, a molecular sieve, or combinations thereof.
  • the separator comprises a flash tank (e.g., flash chamber 200).
  • a flash tank can comprise a vessel configured to vaporize and/or remove low vapor pressure components from a high temperature and/or high pressure fluid.
  • the separator for separating the polymerization product into a polymer stream and a gas stream can be configured such that an incoming stream can be separated into a liquid stream (e.g., a condensate stream) and a gas (e.g., vapor) stream.
  • the liquid stream can comprise a reaction product (e.g., polyethylene, often referred to as "polymer fluff').
  • the liquid stream can be a bottoms stream.
  • the gas or vapor stream can comprise volatile solvents, gaseous, unreacted monomers and/or optional comonomers, waste gases (secondary reaction products, such as contaminants and the like), or combinations thereof.
  • the gas stream can be an overhead stream.
  • the separator for separating the polymerization product into a polymer stream and a gas stream can be configured such that the polymerization product stream is flashed by heat, pressure reduction, or both such that an enthalpy of the polymerization product stream is increased.
  • This can be accomplished via a heater, a flashline heater, various other operations commonly known in the art, or combinations thereof.
  • a flash line heater comprising a double pipe can exchange heat by hot water or steam.
  • Such a flashline heater can increase the temperature of the stream while reducing its pressure.
  • Separating the polymerization product stream into a polymer stream and a gas stream can comprise distilling, vaporizing, flashing, filtering, membrane screening, centrifuging, absorbing, adsorbing, or combinations thereof, the polymerization product.
  • separating the polymerization product stream into a polymer stream and a gas stream yields a gas stream 210 and a polymer stream 220 (e.g., polyethylene polymer, copolymer, etc.).
  • the gas stream 210 can comprise unreacted monomer (e.g., unreacted ethylene monomer), optional unreacted comonomer, and various gases.
  • Gas stream 210 can comprise the non-solid components of polymerization product stream 120 in a vapor phase
  • the gas stream 210 can comprise hydrogen, nitrogen, methane, ethylene, ethane, propylene, propane, butane, isobutane, pentane, hexane, 1-hexene, heavier hydrocarbons, or combinations thereof.
  • the gas stream 210 can further comprise trace amounts of oxygen.
  • ethylene can be present in a range of from 0.1% to 15%, alternatively, from 1.5% to 5%, alternatively, 2% to 4% by total weight of the gas stream.
  • Ethane can be present in a range of from 0.001% to 4%, alternatively, from 0.2% to 0.5% by total weight of the gas stream.
  • Isobutane can be present in a range from 80% to 98%, alternatively, from 92% to 96%, alternatively, 95% by total weight of the gas stream.
  • the mid-polymerization reactor stream 15 can be processed in a similar manner to the polymerization product stream 121, wherein the mid-polymerization reactor stream 15 can be separated into a mid-polymerization polymer stream and a mid-polymerization gas stream.
  • the mid-polymerization polymer stream can be communicated to the second reactor 106; processed in a similar manner to the polymer stream 220, as will be described in more detail later herein; communicated to the purge column 400, such as for example via the polymer stream 220; or combinations thereof.
  • the mid-polymerization gas stream can be processed in a similar manner to the gas stream 210, as will be described in more detail later herein, and/or communicated to the heavy distillation column 300 and/or to the distillation column 301, such as for example via the gas stream 210.
  • the PEP process 2000 can generally comprise the step 2400 of purging the polymer stream to produce a purged polymer stream and a spent purge gas stream.
  • a primary solids feed to the purge column 400 comprises typically the polymer stream 220.
  • the polymer stream 220 comprises a solids discharge (e.g., polyolefin fluff, such as for example polyethylene fluff) that exits the flash chamber 200.
  • a purpose of the purge column 400 is to remove residual hydrocarbon from polymer stream 220 and to provide a substantially-clean polymer fluff (e.g., polymer 425) with relatively small amounts of entrained volatile organic content.
  • the polymer 425 e.g., polymer fluff
  • the polymer 425 can be transported or conveyed to an extrusion/loadout system for conversion to pellets and/or for distribution and sale as polyolefin pellet resin.
  • the polymer stream 220 can comprise a polymer (e.g., polyethylene), unreacted monomer (e.g., ethylene, 1-hexene) and various gases (e.g., ethane, isobutane, hydrogen, methane, propane, butane, pentane, hexane, propylene).
  • a polymer e.g., polyethylene
  • unreacted monomer e.g., ethylene, 1-hexene
  • gases e.g., ethane, isobutane, hydrogen, methane, propane, butane, pentane, hexane, propylene
  • Processing e.g., purging
  • the polymer stream 220 can yield the purged polymer stream 420 and the spent purge gas stream 430 generally comprising a purge gas (e.g., nitrogen), unreacted monomer (e.g., ethylene, 1-hexene), and various gases (e.g., ethane, isobutane, hydrogen, nitrogen, methane, propylene, propane, butane, pentane, hexane, heavier hydrocarbons).
  • a purge gas e.g., nitrogen
  • unreacted monomer e.g., ethylene, 1-hexene
  • gases e.g., ethane, isobutane, hydrogen, nitrogen, methane, propylene, propane, butane, pentane, hexane, heavier hydrocarbons.
  • a purge gas 410 e.g., an inert gas, nitrogen
  • purge column 400 can be circulated through purge column 400 to remove residual hydrocarbons via a spent purge gas stream 430.
  • the spent purge gas stream 430 can be communicated to a separation unit, such as for example an INRU unit, for hydrocarbon separation and/or recovery.
  • purge column 400 can be a cylindrical vessel having a relatively tall vertical section, a cover or head at the top, sloped sides or conical shape at the bottom with an opening for polymer fluff discharge.
  • the polymer fluff to be degassed of volatile hydrocarbons can enter the vessel at the top, while the purge gas, typically nitrogen, can be introduced to the vessel in the sloped bottom sides.
  • Flow can be countercurrent between the purge gas and polymer fluff in the vessel.
  • a hydrocarbon rich purge gas e.g., spent purge gas 430
  • a degassed fluff e.g., purged polymer stream 420
  • Degassing effectiveness in the purge column can be predicated on the maintenance of an uniform plug flow of the polymer fluff and purge gas in the purge column, thereby ensuring good contact between the two.
  • a diameter (D) of the purge column can typically range from 5 to 6 feet, but a length (L) of the purge column can be chosen to achieve a residence time (e.g., from 30 to 180 minutes) sufficient for degassing the polymer fluff.
  • L/D ratios can range from 4 to 8; however, L/D ratios can be outside this range.
  • Internal features can be employed in the purge column, such as a distributor plate for introducing purge gas (e.g., nitrogen), an inverted cone for facilitating plug flow of the polymer (e.g., to reduce bridging or channeling of the polymer fluff), and the like.
  • purge gas e.g., nitrogen
  • an inverted cone for facilitating plug flow of the polymer (e.g., to reduce bridging or channeling of the polymer fluff), and the like.
  • processing the purged polymer stream 420 comprises any suitable process or series of processes configured to produce a polymer product as can be suitable for commercial or industrial usage, storage, transportation, further processing, or combinations thereof.
  • Processing the purged polymer stream 420 can comprise routing the purged polymer stream 420 to a polymer processor.
  • the polymer processor can be configured for the performance of a suitable processing means (e.g., to form various articles), nonlimiting examples of which include cooling, injection molding, melting, pelletizing, film blowing, cast film, blow molding, extrusion molding, rotational molding, thermoforming, cast molding, fiber spinning, and the like, or combinations thereof.
  • Various additives and modifiers can be added to the polymer to provide better processing during manufacturing and for desired properties in the end product.
  • Nonlimiting examples of such additives can include surface modifiers such as slip agents, antiblocks, tackifiers; antioxidants such as primary and secondary antioxidants; pigments; processing aids such as waxes/oils and fluoroelastomers; and/or special additives such as fire retardants, antistats, scavengers, absorbers, odor enhancers, and degradation agents.
  • surface modifiers such as slip agents, antiblocks, tackifiers
  • antioxidants such as primary and secondary antioxidants
  • pigments such as waxes/oils and fluoroelastomers
  • special additives such as fire retardants, antistats, scavengers, absorbers, odor enhancers, and degradation agents.
  • the polymer can include other suitable additives.
  • additives can be used singularly or in combination and can be included in the polymer before, during or after preparation of the polymer as described herein.
  • Such additives can be added via known techniques, for example during an extrusion or compounding step such as during pelletization or subsequent processing into an end use article.
  • the polymer processor can be configured to form a suitable polymer product.
  • suitable polymer products as can result from processing the purged polymer stream include films, powders, pellets, resins, liquids, or any other suitable form as will be appreciated by those of skill in the art.
  • Such a suitable output can be for use in, for example, one or more of various consumer or industrial products.
  • the polymer product can be utilized in any one or more of various articles, including, but not limited to, bottles, drums, toys, containers, household containers, utensils, film products, tanks, fuel tanks, pipes, membranes, geomembranes, and liners.
  • the polymer processor is configured to form pellets for transportation to a consumer product manufacturer.
  • the PEP process 2000 can generally comprise the step 2500 of processing the gas stream in one or more distillation columns to produce a light hydrocarbon stream.
  • processing the gas stream 210 can comprise separating at least one gaseous component from the gas stream. While the step of processing the gas stream will be discussed in detail in the context of two distillation columns used for such processing of the gas stream, it should be understood that any suitable number of distillation columns can be used for processing the gas stream, such as for example one, two, three, four, five, or more distillation columns.
  • Separating at least one gaseous component from the gas stream can comprise distilling a gas stream (e.g., gas stream 210) in one step so as to allow at least one gaseous component to separate from other gaseous components according to temperature(s) of boiling.
  • distillation column 301 can be configured to separate at least one gaseous component from a gas stream (e.g., gas stream 210).
  • the gas stream 210 can be communicated to the distillation column 301.
  • Gas stream 210 can be distilled in the distillation column 301 to form light hydrocarbon stream 304, distillation bottoms stream 302, and distillation side stream 303.
  • the light hydrocarbon stream 304 can comprise ethylene, ethane, optionally hydrogen, or combinations thereof.
  • the light hydrocarbon stream 304 can be communicated to the PSA unit 500.
  • the distillation bottoms stream 302 can comprise hexane, hexene, optionally isobutane, or combinations thereof.
  • the distillation side stream 303 can comprise isobutane.
  • Intermediate hydrocarbon stream 330 can be characterized as comprising, alternatively, comprising substantially, alternatively, consisting essentially of, alternatively, consisting of, C 4 and lighter hydrocarbons (e.g., butane, isobutane, propane, propylene, ethane, ethylene, methane, etc.) and any light gases (e.g., nitrogen).
  • lighter hydrocarbons e.g., butane, isobutane, propane, propylene, ethane, ethylene, methane, etc.
  • any light gases e.g., nitrogen
  • C 4 and lighter hydrocarbons and gases can be present in the intermediate hydrocarbon stream 330 in an amount of from 80% to 100% by total weight of the intermediate hydrocarbon stream, alternatively from 90% to 99.999999%, alternatively from 99% to 99.9999%, alternatively, C 5 and heavier hydrocarbons can be present in the intermediate hydrocarbon stream 330 in an amount from 0% to 20% by total weight of the intermediate hydrocarbon stream, alternatively from 10% to 0.000001%, alternatively from 1.0% to 0.0001%.
  • at least 90% by weight of the C 4 and lighter hydrocarbons and gases of the gas stream 210 can be present in the intermediate hydrocarbon stream 330, alternatively, at least 98%, alternatively, at least 99%.
  • heavy distillation bottoms stream 310 can be characterized as comprising C 6 and heavy components (e.g., C 6 and heavier alkanes and oligomers), wherein the heavy components can comprise alkanes, that is, alkanes larger than hexane (e.g., heptane and/or other large alkanes). Hydrocarbons other than C 6 and heavy alkanes (e.g., C 6 and heavier alkanes and oligomers) can be present in the heavy distillation bottoms stream 310 in an amount less than 15%, alternatively, less than 10%, alternatively, less than 5% by total weight of the heavy distillation bottoms stream 310.
  • the heavy distillation bottoms stream 310 can be directed to additional processing steps or methods, or alternatively they can be disposed of, as appropriate. In an example, the heavy distillation bottoms stream 310 can be incinerated.
  • the heavy distillation side stream 320 can be characterized as comprising hexene.
  • hexene can be present in heavy distillation side stream 320 in an amount of from 20% to 98% by total weight of the heavy distillation side stream 320, alternatively from 40% to 95%, alternatively from 50% to 95%.
  • the heavy distillation side stream 320 can be recycled. Recycling the heavy distillation side stream 320 can comprise routing, for example, via a suitable pump or compressor, the heavy distillation side stream 320 back to and/or introducing the heavy distillation side stream 320 into one or more components of the PEP system 1000, for example, into slurry loop reactor system 100 for reuse in a polymerization reaction. Recycling the heavy distillation side stream 320 can provide an efficient and/or cost-effective means of supplying hexene for operation of the polymerization reaction process. At least a portion of the hexene of the heavy distillation side stream 320 can be employed in the polymerization reaction as, for example, a comonomer in the reaction.
  • At least a portion of the heavy distillation side stream 320 can be routed to storage for subsequent use in a polymerization reaction or employed in any other suitable process.
  • at least a portion of the hexene can be recycled back to the reactor when the reactor is undergoing a polymerization reaction involving hexene as a comonomer.
  • at least a portion of the hexene can be stored when the reactor is undergoing a polymerization reaction in the absence of hexene.
  • At least a portion of the heavy distillation bottoms stream 310 and/or heavy distillation side stream 320 can be returned to the heavy distillation column 300.
  • at least a portion of the heavy distillation bottoms stream 310 and/or heavy distillation side stream 320 can be routed via a reboiler to the heavy distillation column 300 for additional processing.
  • a heavy distillation column 300 can be provided with one or more inlets and at least two outlets.
  • the heavy distillation column 300 can be operated at a suitable temperature and pressure, for example as can be suitable to achieve separation of the components of the gas stream 210.
  • the heavy distillation column 300 can be operated at a temperature in a range of from 15 °C to 233 °C, alternatively, from 20 °C to 200 °C, alternatively, from 20 °C to 180 °C, and/or a pressure in a range of from 14.7 psi to 527.9 psi, alternatively, from 15.7 psi to 348 psi, alternatively, from 85 psi to 290 psi.
  • the heavy distillation column 300 can be configured and/or sized to provide for separation of a suitable volume of gases (e.g., a flash gas stream).
  • a suitable volume of gases e.g., a flash gas stream.
  • the gas stream 210 can remain and/or reside within heavy distillation column 300 for any suitable amount of time, for example an amount of time as can be necessary to provide sufficient separation of the components within the heavy distillation column 300.
  • the gas stream 210 can be introduced into the heavy distillation column 300 without a compressive step, that is, without compression of the gas stream 210 after it is emitted from the flash chamber 200 and before it is introduced into the heavy distillation column 300.
  • the gas stream 210 can be introduced into the heavy distillation column 300 at substantially the same pressure as the outlet pressure of flash chamber 200 (e.g., a pressure of from 14.7 psia to 527.9 psia, alternatively, from 15.7 psia to 348 psia, alternatively, from 85 psia to 290 psia at the outlet of the flash chamber 200).
  • 1 psia corresponds to 6894,76 pascal absolute (i.e actual pressure plus atmospheric pressure).
  • the gas stream 210 can be introduced into the heavy distillation column 300 without a significant compressive step.
  • a compressor e.g., a flash compressor
  • a compressor can be used to raise the pressure of the gas stream 210 to a required level for introducing into heavy distillation column 300.
  • gas stream 210 can be introduced into heavy distillation column 300 at a pressure in a range of from 25 psi less than the pressure at which the gas stream 210 was emitted from the flash chamber 200 to 25 psi greater than the pressure at which the gas stream 210 was emitted from the flash chamber 200, alternatively, from 15 psi less than the pressure at which the gas stream 210 was emitted from the flash chamber 200 to 15 psi greater than the pressure at which the gas stream 210 was emitted from the flash chamber 200, alternatively, from 5 psi less than the pressure at which the gas stream 210 was emitted from the flash chamber 200 to 5 psi greater than the pressure at which the gas stream 210 was emitted from the flash chamber 200.
  • the gas stream 210 can be introduced into the heavy distillation column 300 at a pressure in a range of from 14.7 psia to 527.8 psia, alternatively, from 15.7 psia to 348 psia, from 85 psia to 290 psia.
  • the heavy distillation column 300 can be configured and/or operated such that each of the intermediate hydrocarbon stream 330, the heavy distillation bottoms stream 310, and an optional heavy distillation side stream 320 can comprise a desired portion, part, or subset of components of the gas stream 210.
  • the location of a particular stream outlet, the operating parameters of the heavy distillation column 300, the composition of the gas stream 210, or combinations thereof can be manipulated such that a given stream can comprise a particular one or more components of the gas stream 210.
  • the intermediate hydrocarbon stream 330 can be separated in the light distillation column 350 to form light hydrocarbon stream 380, light distillation bottoms stream 360, and optionally, light distillation side stream 370.
  • At least one gaseous component can be emitted from the light distillation column 350 in light hydrocarbon stream 380, and the other gaseous components can be emitted from the light distillation column 350 in light distillation bottoms stream 360.
  • light hydrocarbon stream 380 can be characterized as comprising ethylene and ethane.
  • ethylene can be present in light hydrocarbon stream 380 in an amount from 30% to 99% by total weight of the light hydrocarbon stream 380, alternatively from 40% to 98%, alternatively from 60% to 98%, alternatively from 50% to 95%, alternatively from 70% to 95%, or alternatively from 70% to 90%.
  • ethane can be present in light hydrocarbon stream 380 in an amount from 1% to 70% by total weight of the light hydrocarbon stream 380, alternatively from 2% to 60%, alternatively from 2% to 40%, alternatively from 5% to 50%, alternatively from 5% to 30%, or alternatively from 10% to 30%.
  • the light hydrocarbon stream 380 can further comprise other light gases (e.g., methane, carbon dioxide, nitrogen, hydrogen, or combinations thereof).
  • other light gases e.g., methane, carbon dioxide, nitrogen, hydrogen, or combinations thereof.
  • Light distillation bottoms stream 360 can be characterized as comprising propane, butane, isobutane, pentane, hexane, heavier saturated hydrocarbons, or combinations thereof.
  • the light distillation bottoms stream 360 can be free of olefins, alternatively, substantially free of olefins, alternatively, essentially free of olefins, alternatively, consisting essentially of or consisting of non-olefins.
  • olefins can be present in light distillation bottoms stream 360 in an amount of less than 1.0% by total weight of the light distillation bottoms stream 360, alternatively, less than 0.5%, alternatively, less than 0.1%.
  • the light distillation bottoms stream 360 can comprise olefin-free isobutane 365.
  • the light distillation side stream 370 can be characterized as comprising isobutane.
  • light distillation side stream 370 comprising, alternatively, consisting of or essentially consisting of, isobutane can be emitted from the light distillation column 350.
  • the isobutane of light distillation bottoms stream 360 can comprise a different grade of isobutane than the isobutane of light distillation side stream 370.
  • light distillation bottoms stream 360 can comprise isobutane that is substantially free of olefins
  • light distillation side stream 370 can comprise a recycle isobutane which can include olefins.
  • At least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 can be recycled.
  • recycling at least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 can comprise routing, for example, via a suitable pump or compressor, at least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 back to and/or introducing at least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 into one or more components of the PEP system 1000, for example, into slurry loop reactor system 100 for reuse in a polymerization reaction.
  • At least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 can be combined with various other components (catalysts, cocatalysts, etc.) to form a catalyst slurry that can be introduced into one or more of reactors 104, 106.
  • the light distillation bottoms stream 360 can be mixed with catalytic components (e.g., catalysts, cocatalysts, etc.) without the risk of unintended polymerization reactions (e.g., polymerization prior to introduction into the one or more reactors).
  • At least a portion of light distillation bottoms stream 360 can serve as a source of olefin-free isobutane for a polymerization reaction. Recycling at least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 can provide an efficient and/or cost-effective means of supplying isobutane for operation of the polymerization reaction process. In an alternative example, at least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 can be routed to storage for subsequent use in a polymerization reaction or employed in any other suitable process.
  • At least a portion of the light distillation bottoms stream 360 can be recycled to a PSA unit, for example via a sweeping gas stream (e.g., sweeping gas stream 510).
  • the light distillation bottoms stream 360 comprising olefin-free isobutane 365 can be recycled 366 to the PSA unit 500, for example via the sweeping gas stream 510, as shown in Figure 1A and/or Figure 1B .
  • At least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 can be routed to storage for subsequent use in any suitable process.
  • At least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 can be returned to the light distillation column 350.
  • at least a portion of the light distillation side stream 370 and/or light distillation bottoms stream 360 can be routed via a reboiler to the light distillation column 350 for additional processing.
  • the light distillation column 350 can be configured and/or sized to provide for separation of a suitable volume of gases.
  • the light distillation column 350 can be operated at a temperature in a range of from 50 °C to -35 °C, alternatively, from 50 °C to -30 °C, alternatively, from 50 °C to -20 °C, alternatively, from 50 °C to -10 °C, alternatively, from 50 °C to 0 °C, alternatively, from 50 °C to 10 °C, alternatively, from 50 °C to 20 °C, alternatively, from 40 °C to 10 °C, alternatively, from 30 °C to 5 °C, and a pressure in a range of from 14.7 psia to 529.7 psia, alternatively, from 15.7 psia to 348 psia, alternatively, from 85 psia to 290 psia.
  • the light distillation column 350 can be configured and/or sized to provide for separation of a suitable volume of intermediate hydrocarbon stream 330. As will be appreciated by one of skill in the art, the intermediate hydrocarbon stream 330 can remain and/or reside within light distillation column 350 for any suitable amount of time as can be necessary to provide sufficient separation of the components of intermediate hydrocarbon stream 330. In an example, light distillation column 350 can be provided with at least two outlets.
  • the light distillation column 350 can be configured and/or operated such that each of light hydrocarbon stream 380 and the light distillation bottoms stream 360 can comprise a desired portion, part, or subset of components of the intermediate hydrocarbon stream 330.
  • each of light hydrocarbon stream 380 and the light distillation bottoms stream 360 can comprise a desired portion, part, or subset of components of the intermediate hydrocarbon stream 330.
  • the location of a particular stream inlet or outlet, the operating parameters of the light distillation column 350, the composition of the intermediate hydrocarbon stream 330, or combinations thereof can be manipulated such that a given stream can comprise a particular one or more components of the intermediate hydrocarbon stream 330.
  • the PEP process 2000 comprises the step 2600 of contacting the light hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream.
  • At least one gaseous component e.g., ethylene
  • ethylene can be separated from the light hydrocarbon stream 380 during step 2600.
  • Separating at least one gaseous component from a gas stream generally comprises any suitable method of selectively separating at least a first chemical component or compound from a stream comprising the first chemical component or compound and one or more other chemical components, compounds, or the like.
  • the gaseous component separated from the gas stream can comprise one or more hydrocarbons.
  • hydrocarbons include alkanes (e.g., ethane, butane, isobutane, hexane, and the like, or combinations thereof) and alkenes or olefin monomers (e.g., ethylene) or optional comonomers.
  • the gaseous component separated from the gas stream can comprise an unreacted hydrocarbon monomer, e.g., ethylene.
  • the gaseous component separated from the gas stream can comprise an unreacted hydrocarbon comonomer.
  • the gaseous component separated from the gas stream can comprise an unreacted hydrocarbon monomer (e.g., ethylene, alone or in combination with other hydrocarbons, such as, ethane, isobutane, hexane, or combinations thereof), or optionally, hydrocarbon comonomer alone or in combination with other hydrocarbons, such as, ethane, isobutane, hexane, or combinations thereof.
  • the gaseous component separated from the gas stream can comprise ethane.
  • suitable separating means include distilling, vaporizing, flashing, filtering, membrane screening, absorbing, adsorbing, molecular weight exclusion, size exclusion, polarity-based separation, and the like, or combinations thereof.
  • At least one gaseous component can be separated from the light hydrocarbon stream 380 and/or light hydrocarbon stream 304 by pressure swing adsorption (PSA), thereby enabling ethylene recovery, as will be described in more detail herein.
  • PSA pressure swing adsorption
  • separating ethane from a gas stream e.g., light hydrocarbon stream 380, light hydrocarbon stream 304, etc.
  • adsorbing ethane in a PSA unit enables the recovery of ethylene as recovered or non-adsorbed ethylene, such as for example as part of a non-adsorbed gas stream.
  • Recovering ethylene from the light hydrocarbon stream 380 and/or 304 can generally comprise contacting the light hydrocarbon stream 380 and/or 304 with a purged hydrocarbon adsorber in a PSA unit 500 to yield a loaded hydrocarbon adsorber generally comprising adsorbed ethane, and a non-adsorbed gas stream 520 generally comprising ethylene (e.g., recovered or non-adsorbed ethylene).
  • the non-adsorbed gas stream 520 can further comprise other light gases (e.g., methane, carbon dioxide, nitrogen, hydrogen, or combinations thereof) that were present in the light hydrocarbon stream 380 and/or 304.
  • the non-adsorbed gas stream 520 can generally comprise ethylene, isobutane, and nitrogen; alternatively ethylene and isobutane; or alternatively ethylene and nitrogen.
  • the term "loaded” when used to describe or when referring to a hydrocarbon adsorber is intended to be nonlimiting, and is intended to denote (e.g., mean, signify, indicate, represent, etc.) that the hydrocarbon adsorber has an amount of a hydrocarbon (e.g., ethane) adsorbed therein (e.g., adsorbed ethane).
  • the term "loaded” when used to describe a hydrocarbon adsorber is intended to include any amount of an adsorbed hydrocarbon, such as for example an amount of adsorbed hydrocarbon of equal to or greater than 10%, alternatively equal to or greater than 15%, alternatively equal to or greater than 20%, alternatively equal to or greater than 25%, alternatively equal to or greater than 30%, alternatively equal to or greater than 40%, alternatively equal to or greater than 50%, alternatively equal to or greater than 60%, alternatively equal to or greater than 70%, alternatively equal to or greater than 80%, alternatively equal to or greater than 90%, alternatively equal to 100%, based on adsorption capacity of the hydrocarbon adsorber at a given pressure (e.g., first pressure).
  • a given pressure e.g., first pressure
  • the adsorption capacity of the hydrocarbon adsorber at a given pressure can be defined as the ratio of the maximum amount of hydrocarbon that can be adsorbed by the hydrocarbon adsorber to the amount of hydrocarbon adsorber present in the PSA unit, and it can be expressed in g adsorbed hydrocarbon/g hydrocarbon adsorber.
  • adsorbed hydrocarbon refers to a hydrocarbon (e.g., ethane) that is adsorbed or associated with an adsorbent (e.g., adsorbent associated hydrocarbon) in a reversible fashion, wherein the adsorbent is a hydrocarbon adsorber of the type disclosed herein.
  • adsorbent e.g., adsorbent associated hydrocarbon
  • the loaded hydrocarbon adsorber can be a partially loaded hydrocarbon adsorber, wherein the partially loaded hydrocarbon adsorber can comprise an amount of adsorbed hydrocarbon of from 10% to 50%, alternatively from 15% to 45%, or alternatively from 20% to 40%, based on the adsorption capacity of the hydrocarbon adsorber at the first pressure.
  • the loaded hydrocarbon adsorber can be a substantially loaded hydrocarbon adsorber, wherein the substantially loaded hydrocarbon adsorber can comprise an amount of adsorbed hydrocarbon of from 50% to 99%, alternatively from 55% to 95%, or alternatively from 60% to 90%, based on the adsorption capacity of the hydrocarbon adsorber at the first pressure.
  • the loaded hydrocarbon adsorber can be a completely or fully loaded hydrocarbon adsorber (alternatively referred to as a saturated hydrocarbon adsorber), wherein the completely loaded hydrocarbon adsorber can comprise an amount of adsorbed hydrocarbon of 100%, alternatively 99.5%, or alternatively 99%, based on the adsorption capacity of the hydrocarbon adsorber at the first pressure.
  • the hydrocarbon adsorber can undergo an adsorption step (e.g., the hydrocarbon adsorber can adsorb or load a compound) to yield a loaded hydrocarbon adsorber, such as for example a substantially loaded hydrocarbon adsorber or a completely loaded hydrocarbon adsorber, and subsequently the loaded hydrocarbon adsorber (e.g., substantially loaded hydrocarbon adsorber, completely loaded hydrocarbon adsorber) can undergo a desorption step (e.g., the hydrocarbon adsorber can desorb or unload a compound) to yield an unloaded hydrocarbon adsorber or a partially loaded hydrocarbon adsorber.
  • an adsorption step e.g., the hydrocarbon adsorber can adsorb or load a compound
  • the hydrocarbon adsorber can be characterized by a first adsorption capacity at the first pressure, and by a second adsorption capacity at a second pressure, wherein the first pressure is greater than the second pressure, and wherein the first adsorption capacity is greater than the second adsorption capacity, thereby enabling an adsorption or loading step at the first pressure and a desorption or unloading step at the second pressure.
  • Separating at least one gaseous component from the light hydrocarbon stream can comprise contacting the light hydrocarbon stream with an adsorbent (e.g., hydrocarbon adsorber, purged hydrocarbon adsorber as disclosed herein), for example, so as to allow the gaseous component to be adsorbed by the adsorbent.
  • separating at least one gaseous component from the light hydrocarbon stream comprises selectively adsorbing the at least one gaseous component from a light hydrocarbon stream.
  • adsorbing the at least one gaseous component from the light hydrocarbon stream generally comprises contacting the light hydrocarbon stream with a suitable adsorbent, allowing the at least one component to be adsorbed by the adsorbent, and, recovering a stream comprising unadsorbed gases (e.g., non-adsorbed gas stream 520), such as for example recovered or non-adsorbed ethylene.
  • separating at least one gaseous component from the light hydrocarbon stream can further comprise liberating the adsorbed gaseous component from the adsorbent (e.g., recovered adsorbed gas stream 530), such as for example liberating ethane.
  • the hydrocarbon adsorber comprises a substance, material and/or compound capable of facilitating adsorption and desorption of a hydrocarbon (e.g., ethane) from a hydrocarbon mixture (e.g., light hydrocarbon stream) by way of a pressure swing adsorption process.
  • a hydrocarbon e.g., ethane
  • the hydrocarbon adsorber can comprise a substance, material and/or compound capable of adsorbing hydrocarbons, preferably in a selective manner.
  • the hydrocarbon adsorber can comprises any material capable of selectively adsorbing one or more hydrocarbon components of a gas mixture (e.g., a light hydrocarbon stream).
  • the hydrocarbon adsorber can selectively adsorb one or more hydrocarbons at a first pressure, and can selectively desorb (e.g., regenerate, unload) one or more hydrocarbons at a second pressure, wherein the first pressure is greater than the second pressure.
  • the hydrocarbon adsorber comprises a zeolitic imidazolate framework (ZIF).
  • ZIFs are a subclass or subfamily of metal organic frameworks (MOFs), wherein the ZIFs display exceptional thermal stability.
  • MOFs metal organic frameworks
  • ZIFs comprise tetrahedrally-coordinated metal ions connected by organic imidazole linkers.
  • ZIFs are named for the resemblance of their metal-imidazolate-metal bond angles to Si-O-Si angles in zeolites.
  • ZIFs are generally thought to combine the high stability of inorganic zeolites with the high porosity and organic functionality of MOFs.
  • ZIFs are defined as microporous crystalline structures having framework topologies commonly found in zeolites and/or in other crystalline materials wherein each vertex of a framework structure is comprised of a single metal ion and each pair of connected adjacent vertices of the framework structure is linked by nitrogen atoms of an imidazolate anion or a derivative of an imidazolate anion.
  • the ZIF framework structure defines ZIF cages/cavities/pores.
  • microporous when used to describe or when referring to a ZIF is defined as having a pore window size of less than 2.0 nm or 20 Angstroms.
  • a pore window of a ZIF refers to an opening or "window" that diffusing molecules have to pass through in order to diffuse from one ZIF cage/cavity/pore to an adjacent ZIF cage.
  • a pore window size of a ZIF is a geometric parameter that refers to the diameter of the window that connects adjacent ZIF cages that allows the passage of diffusing molecules from one ZIF cage to an adjacent ZIF cage.
  • Nonlimiting examples of metals suitable for use in the present disclosure as part of ZIF structures include Zn, Co, Ni, Fe, Cu, Mg, and the like, or combinations thereof.
  • Nonlimiting examples of ZIFs suitable for use as hydrocarbon adsorbers in the present disclosure include ZIF-7, ZIF-8, ZIF-65, ZIF-67, or combinations thereof.
  • the ZIF can be characterized by a pore window size of from 0.2 nm to 0.5 nm, alternatively from 0.25 nm to 0.45 nm, or alternatively from 0.3 nm to 0.4 nm.
  • ZIF materials can be regarded as having a certain degree of framework flexibility.
  • ZIF cages are interconnected and comprise windows to allow hydrocarbons to enter the ZIF cages and be adsorbed in such cages.
  • the pore window size can be such that only certain hydrocarbons will be able to enter through the window and be adsorbed within the cages.
  • certain ZIFs can exhibit a gate-opening effect upon exposure to a hydrocarbon mixture, such as for example an ethane/ethylene mixture, leading to the selective hydrocarbon (e.g., ethane) adsorption on certain ZIFs.
  • a hydrocarbon mixture such as for example an ethane/ethylene mixture
  • the hydrocarbon adsorber suitable for use in the present disclosure comprises particles (e.g., hydrocarbon adsorber particles, ZIF particles) of any suitable geometry, including without limitation particles, pellets, beads, hollow beads, spheres, ovals, fibers, hollow fibers, tubes, hollow tubes, rods, platelets, disks, plates, ribbons, and the like, or combinations thereof.
  • the hydrocarbon adsorber can be characterized by a particle size of from 0.1 mm to 5 mm, alternatively from 0.2 mm to 2.5 mm, or alternatively from 0.25 mm to 1 mm.
  • the hydrocarbon adsorber further comprises a support, wherein the ZIF contacts at least a portion of the support, is distributed throughout the support, or combinations thereof, and whereby the ZIF is structurally supported by the support.
  • the ZIF can be disposed about the support.
  • the ZIF can be associated with the support.
  • the support can be comprised of any suitable material and/or of any suitable construction and can be porous or non-porous. In some examples, the support can be comprised entirely of a ZIF. In other examples, the support can be comprised entirely of a (relatively) non-adsorbent material towards hydrocarbons.
  • the support has a porosity of from 0 vol.% to 99 vol.%, alternatively from 1 vol.% to 90 vol.%, or alternatively from 10 vol.% to 75 vol.%, based on the total volume of the support.
  • the support has an open cell pore structure, such that ZIFs could be deposited inside the pores of the support, thereby providing a larger surface area for hydrocarbon adsorption.
  • an open cell structure refers to a structure characterized by a high porosity, low density material typically containing pores that are connected to each other.
  • a support open cell structure also enables the unhindered flow of gaseous mixtures (e.g., hydrocarbon mixtures, light hydrocarbon stream, etc.) through the support, and as such the gaseous mixture may efficiently contact the ZIFs.
  • gaseous mixtures e.g., hydrocarbon mixtures, light hydrocarbon stream, etc.
  • the support could provide certain properties that could facilitate the pressure swing adsorption process, such as for example enhanced (e.g., faster) heat transfer.
  • the support could also provide for an enhanced surface area.
  • the support can contact a ZIF, wherein the ZIF comprises a layer or coating on the support; wherein the ZIF can be embedded within the structure of the support; and the like; or combinations thereof.
  • the support comprises a support outer surface, wherein at least a portion of the support outer surface can be in contact with the ZIF.
  • the ZIF can form a ZIF layer contacting the support outer surface.
  • the ZIF layer can be characterized by a thickness effective to enable the pressure swing adsorption process, e.g., adsorption step, desorption step, purging step.
  • the thickness of the ZIF layer could depend on the technique used to deposit ZIF particles onto the support, ZIF particle size distribution, etc.
  • the ZIF layer can be characterized by a thickness of from 10 nm to 5 mm, alternatively from 100 nm to 1 mm, alternatively from 500 nm to 500 microns, alternatively from 500 nm to 250 microns, or alternatively from 1 micron to 100 microns.
  • the support comprises a film, a foil, a mesh, a fiber cloth, a woven fiber mesh, a woven wire mesh, a metallic woven wire mesh, a polymeric membrane, a surface treated material, a surface treated metal foil, a woven fiber cloth, a foam, a polymeric foam, polymeric foam particles, and the like, or combinations thereof.
  • the support can be a woven fiber cloth or fiber mesh wherein at least a fraction of fibers are comprised of a ZIF and wherein the remaining fraction is comprised of a non-adsorbent material.
  • the hydrocarbon adsorber can also be comprised of ZIF crystals or crystallites embedded within the support.
  • the dimensions (e.g., thickness) of a support layer can be any effective dimensions.
  • the effective dimensions of a support represents any dimensions (e.g., thickness) capable of providing at least a minimum integrity needed under PSA process conditions for an intended overall structure of a hydrocarbon adsorber bed comprising a hydrocarbon adsorber.
  • the support comprises a non-adsorbent material towards hydrocarbons.
  • the support can be treated by any suitable treating technique to incorporate at least an effective amount of a ZIF on/within the support material.
  • suitable treating techniques for applying a ZIF to the support suitable for use in the present disclosure include wash coating techniques, in situ crystallization methods that deposit a ZIF directly onto the support from a synthesis solution, doctor-blading, spraying, spray-coating, electrodeposition, dry-wet spinning, or the like.
  • the support can be coated with a ZIF by wash-coating.
  • a typical wash-coating process involves a slurry preparation (e.g., ZIF particles, a suitable binder, and optionally a viscosifying agent), slurry application by washing or dipping, drying, and/or sintering. Once a wet coating is formed, such coating has to be dried and sintered at relatively high temperatures (e.g., from 300 °C to 600 °C) to establish binding among coating components and adhesion between coating and a surface of the support.
  • relatively high temperatures e.g., from 300 °C to 600 °C
  • the hydrocarbon adsorber can further comprise a binder, wherein the binder can facilitate adherence between the ZIF and the support.
  • binders suitable for use in the present disclosure include a crystalline polymer, a non-crystalline polymer, an epoxy, a thermoplastic polymer, a clay, a silica-containing material, an alumina-containing material, a titania-containing material, and the like, or combinations thereof.
  • the binder can have a porous structure.
  • the support comprises a porous material (e.g., a foamed material) and the ZIF can be applied in a manner in which particles of ZIF fill at least a portion of the pores of a porous structure of the support.
  • a slurry containing ZIF crystals can be soaked into, or pressured through, a porous support material, then such support can be dried and/or calcined (e.g., heated to high temperatures, for example greater than 300 °C).
  • a coated support when the support is in a layer form, can typically have two major opposing support surfaces, and one or both of these surfaces can be coated with the ZIF.
  • the hydrocarbon adsorber can further comprise additives.
  • additives can be used to improve the adsorption/desorption and transport properties of hydrocarbons within the ZIF.
  • Nonlimiting examples of additives suitable for use in the present disclosure in the hydrocarbon adsorbers include zeolites, microporous crystalline materials, silicates, silicoaluminophosphates (SAPOs), aluminophosphates (AlPOs), high heat capacity materials, high heat conductivity materials, metals, thermally conductive polymers, a porous thermally conductive polymers, foamed thermally conductive polymers, and the like, or combinations thereof.
  • high heat capacity materials and/or high heat conductivity materials can assist in the capture and transfer of at least a portion of the heat that could be generated during adsorption step(s) of the swing adsorption process, thereby decreasing the duration of cycling process, increasing throughput, and further improving the overall efficiency of the ZIF for selective adsorbtion of desired hydrocarbons (e.g., ethane).
  • desired hydrocarbons e.g., ethane
  • the ZIF when the support is a porous thermally conductive polymer and/or a foamed thermally conductive polymer, the ZIF can be present in the pores of such porous and/or foamed support material, whereby the ZIF is structurally supported by the support.
  • the variation in temperature within a hydrocarbon adsorber bed is not expected to be significant, and as such the presence of high heat capacity materials and/or high heat conductivity materials within the hydrocarbon adsorber could mitigate the effects of any heat released during an adsorption step, without the need to cool the hydrocarbon adsorber bed.
  • the hydrocarbon adsorber bed can be cooled (e.g., external cooling, jacket cooling, internal cooling, coil cooling, etc.).
  • the PSA unit 500 can comprise a hydrocarbon adsorber bed, wherein the hydrocarbon adsorber bed comprises a hydrocarbon adsorber.
  • the hydrocarbon adsorber bed can be assembled by using any suitable methodology compatible with materials and methods disclosed herein.
  • each PSA unit can comprise more than one hydrocarbon adsorber bed, such as for example, two, three, four, five, six, seven, eight, nine, ten, or more hydrocarbon adsorber beds.
  • all hydrocarbon adsorber beds within the same PSA unit undergo the same step at the same time, whether the step is an adsorption step, a desorption step, or a purging step.
  • hydrocarbon adsorber beds within the same PSA unit could be segregated (e.g., separated, partitioned, isolated, etc.) in such a manner that different hydrocarbon adsorber beds within the same PSA unit would undergo different steps during the same time frame. For example, within the same PSA unit, some beds would undergo an adsorption step, while other beds would undergo a desorption step, while some other beds would undergo a purging step, etc.
  • a PSA unit denotes a collection of processing equipment that is designed to perform the required steps, such as for example an adsorption step, a desorption step, a purging step, etc.
  • one PSA unit can include one or more hydrocarbon adsorber beds, wherein the hydrocarbon adsorber beds could have different configurations, such as for example the beds could be arranged in series, in parallel, or combinations thereof.
  • beds can refer to an actual assemblage of material (e.g., hydrocarbon adsorber material).
  • the terms "bed” and "unit” should not be construed as limiting and these terms could be used interchangeably for purposes of the disclosure herein.
  • alternative configurations to the PSA unit and bed configurations specifically disclosed herein are possible and such alternative configurations are within the scope of the present disclosure.
  • the PSA unit comprises a PSA unit structure wherein one or more hydrocarbon adsorber beds can be housed, and wherein the PSA unit structure can have any suitable geometry.
  • the PSA unit structure can have a cylindrical geometry.
  • the hydrocarbon adsorber bed can be characterized by a bed thickness of from 0.1 feet(ft) to 20 ft, alternatively from 1 ft to 20 ft, or alternatively from 2 ft to 10 ft.
  • the PSA unit can comprise a gas mixture inlet and a gas mixture outlet.
  • open flow channels can be provided through the hydrocarbon adsorber bed or beds for the flow of gaseous mixtures (e.g., light hydrocarbon stream, a sweeping gas stream, etc.), wherein the open flow channels can be continuous between the gas mixture inlet and the gas mixture outlet of the PSA unit.
  • Open flow channels can comprise structurally added elements to the PSA unit, such as for example perforated tubes that enable gas flow, spacers, etc.; spaces between hydrocarbon adsorber particles; hydrocarbon adsorber pores; support pores; etc.
  • the gas mixture inlet and the gas mixture outlet can be located on a body of the PSA unit structure between two opposite ends of such PSA unit structure. In other examples, the gas mixture inlet and the gas mixture outlet can be located on substantially opposite ends of the PSA unit structure. In some other examples, the gas mixture inlet and the gas mixture outlet can be located in any suitable location on the PSA unit structure.
  • a PSA unit structure can comprise spacers.
  • spacers can provide a fixed distance between layers or sheets of a structure, such as for example between layers of hydrocarbon adsorbers, between hydrocarbon adsorber beds, etc.
  • the spacers can be either integral to the hydrocarbon adsorber bed, of they can be a non-integral independent material.
  • the spacers could be formed during assembling of the hydrocarbon adsorber bed, such as dimples or corrugations (e.g., within the support) of a predetermined size to provide a desired flow channel volume of the open flow channels.
  • the spacers can be comprised of any suitable material that can be relatively inactive in the PSA unit and that should not typically decompose under PSA process conditions.
  • suitable spacer materials suitable for use in the present disclosure include particles, such as glass microspheres, wires of suitable size, and the like, or combinations thereof.
  • the PSA unit can comprise a PSA unit structure filled with hydrocarbon adsorber particles, wherein the hydrocarbon adsorber particles are contained within the PSA unit structure, such as for example with the help of screens.
  • a size of a screen opening is smaller than a size of the hydrocarbon adsorber particles.
  • the PSA unit can comprise a stacked layered sheet structure.
  • the stacked layered sheet structure can be assembled by first preparing a single layer substructure, then folding it back and forth on itself multiple times until a final desired stacked layered sheet structure can be achieved.
  • the stacked layered sheet structure can be assembled by simply stacking single layer substructures.
  • a layer of hydrocarbon adsorber can be applied to a sheet of support, as previously described herein.
  • the PSA unit can comprise a plurality of support layers.
  • the PSA unit can further comprise spacers, wherein the spacers can define open flow channels.
  • a distance between the support layers can be defined by the dimensions of the spacers.
  • the PSA unit can comprise a support in a corrugated form, wherein the support comprises folds or furrows.
  • the support comprises folds or furrows.
  • either one or both sides of the corrugated support can comprise the hydrocarbon adsorber.
  • Open flow channels can be formed between two opposing corrugated support layers.
  • PSA units rely on pressure swing adsorption (PSA) as a process for selectively separating at least one gaseous component from a gas mixture (e.g., hydrocarbon mixture, light hydrocarbon stream, etc.).
  • PSA processes rely on the fact that under pressure gases tend to be adsorbed within a pore structure of a porous or microporous adsorbent material (e.g., hydrocarbon adsorber, ZIF, etc.).
  • PSA utilizes a solid adsorbent material (e.g., hydrocarbon adsorber, ZIF, etc.) that preferentially retains or adsorbs a more readily adsorbed component (e.g., a first hydrocarbon, ethane, etc.) relative to a less readily adsorbed component (e.g., a second hydrocarbon, ethylene, etc.) of a gas mixture (e.g., hydrocarbon mixture, light hydrocarbon stream, etc.).
  • a solid adsorbent material e.g., hydrocarbon adsorber, ZIF, etc.
  • a more readily adsorbed component e.g., a first hydrocarbon, ethane, etc.
  • a less readily adsorbed component e.g., a second hydrocarbon, ethylene, etc.
  • a gas mixture e.g., hydrocarbon mixture, light hydrocarbon stream, etc.
  • PSA processes when operated under certain conditions, allow a selective component or components (e.g., first hydrocarbon, ethane) in a gas mixture to be preferentially adsorbed within the pore structure of porous adsorbent materials (e.g., hydrocarbon adsorber, ZIF) relative to a second component or components (e.g., second hydrocarbon, ethylene) in the gas mixture.
  • a selective component or components e.g., first hydrocarbon, ethane
  • porous adsorbent materials e.g., hydrocarbon adsorber, ZIF
  • An adsorption capacity and/or a selectivity of adsorption for a specific component over another component (i.e., adsorption selectivity) as related to a specific hydrocarbon adsorber can often be improved by operating the PSA process under specific pressure and temperature conditions since both pressure and temperature could influence the adsorption properties of the hydrocarbon adsorbers to a certain extent.
  • gas adsorption within an adsorption bed is generally an exothermic process, thereby causing a rise in temperature during such adsorption.
  • the rise in temperature during an adsorption step of a PSA process is generally minimal due to the high pressure under which the adsorption step occurs.
  • the hydrocarbon adsorber bed can be cooled during an adsorption step.
  • the pressure in the PSA unit can be decreased, thereby causing the desorption of the adsorbed gases.
  • PSA processes can be used to separate gases in a mixture when used with an adsorbent (e.g., hydrocarbon adsorber, ZIF) that is selective for one or more of the components of a gas mixture.
  • an adsorbent e.g., hydrocarbon adsorber, ZIF
  • PSA and temperature swing adsorption (TSA) processes could be used in conjunction with each other.
  • a combined PSA/TSA process can be utilized, for example, by increasing the temperature of the adsorbent materials during the lower pressure purge step of a conventional PSA process to improve the desorption of selectively adsorbed component(s) in the process.
  • a bed temperature can then be reduced (or allowed to be reduced, e.g., allowed to cool) during the adsorption step of a PSA cycle to improve adsorption characteristics of the adsorbent material.
  • a hydrocarbon adsorber bed (e.g., hydrocarbon adsorber) can be repeatedly cycled through at least two steps: an adsorption/loading step and a desorption/unloading step (e.g., pressure assisted desorption step). Regeneration or unloading of the hydrocarbon adsorber bed can be achieved by decreasing the pressure within the PSA unit to a pressure effective in desorbing at least a portion of the gas or gases that were adsorbed by the hydrocarbon adsorber during the adsorption step.
  • the PSA process can be conducted with rapid cycles, in which case it can be referred to as a rapid cycle pressure swing adsorption (RCPSA) process.
  • RCPSA rapid cycle pressure swing adsorption
  • the pressure swing adsorption unit can be characterized by a cycle time of from 10 seconds to 1 hour, alternatively from 10 seconds to 50 minutes, alternatively from 15 seconds to 40 minutes, alternatively from 20 seconds to 30 minutes, alternatively from 25 seconds to 20 minutes, or alternatively from 30 seconds to 10 minutes.
  • the cycle time of the PSA unit can be defined as the time between the start of two successive adsorption steps, e.g., a time frame necessary to complete an adsorption step, a desorption step and a purging step that are consecutive.
  • a PSA process can be conducted in a PSA unit comprising a hydrocarbon adsorber bed, wherein the hydrocarbon adsorber bed comprises a ZIF, wherein the first hydrocarbon comprises a saturated hydrocarbon (e.g., ethane), wherein the second hydrocarbon comprises an olefin (e.g., ethylene).
  • a hydrocarbon adsorber bed comprises a ZIF
  • the first hydrocarbon comprises a saturated hydrocarbon (e.g., ethane)
  • the second hydrocarbon comprises an olefin (e.g., ethylene).
  • a partial pressure of the first hydrocarbon during the adsorption step is higher than a partial pressure of the first hydrocarbon during the desorption step, thereby allowing for the recovery of at least a portion of the first hydrocarbon during the desorption step and for the regeneration of the hydrocarbon adsorber by depletion of adsorbed components, wherein the regenerated hydrocarbon adsorber can be re-used in a subsequent adsorption step.
  • Lowering the partial pressure of the first hydrocarbon can be accomplished by lowering a total pressure in the PSA unit (e.g., a total pressure that the hydrocarbon adsorber bed is subjected/exposed to; a second pressure) during the desorption step, when compared to a total pressure in the PSA unit during the adsorption step (e.g., a total pressure that the hydrocarbon adsorber bed is subjected/exposed to; a first pressure).
  • a total pressure in the PSA unit e.g., a total pressure that the hydrocarbon adsorber bed is subjected/exposed to; a second pressure
  • the PSA process can comprise an adsorption step (e.g., a loading step), a desorption step (e.g., an unloading step), and a purging step.
  • the adsorption step e.g., step 2600 of contacting the light hydrocarbon stream with a purged hydrocarbon adsorber
  • the desorption step e.g., step 2700 of contacting the loaded hydrocarbon adsorber with a sweeping gas stream
  • a purging step e.g., step 2800 of contacting the hydrocarbon adsorber with the sweeping gas stream
  • the first pressure can be in the range of from 600 kPa to 3,000 kPa, alternatively from 1,000 kPa to 2,700 kPa, or alternatively from 1,500 kPa to 2,500 kPa.
  • the second pressure can be in the range of from 10 kPa to 500 kPa, alternatively from 50 kPa to 150 kPa, or alternatively from 75 kPa to 125 kPa.
  • the first pressure is greater than the second pressure by equal to or greater than 400 kPa, alternatively by greater than 1,000 kPa, or alternatively by greater than 2,000 kPa.
  • the PSA process (e.g., adsorption step, desorption step, purging step) can occur at a temperature of from -30 °C to 50 °C, alternatively from -25 °C to 30 °C, or alternatively from -20 °C to 25 °C.
  • the temperature of the PSA process is considered not to vary significantly over the course of a cycle, e.g., the temperature of the PSA process does not vary in a manner that interferes with performing the adsorption step, the desorption step, and/or the purging step.
  • the adsorption step can be characterized by an initial temperature (e.g., a temperature at the beginning of the adsorption step) and a final temperature (e.g., a temperature at the end of the adsorption step).
  • a difference between an initial temperature and a final temperature, wherein the smaller value is subtracted from the larger value can be less than 25 °C, alternatively less than 20 °C, alternatively less than 15 °C, alternatively less than 10 °C, alternatively less than 9 °C, alternatively less than 8 °C, alternatively less than 7 °C, alternatively less than 6 °C, alternatively less than 5 °C, alternatively less than 4 °C, alternatively less than 3 °C, alternatively less than 2 °C, or alternatively less than 1 °C.
  • the light hydrocarbon stream can be contacted with a hydrocarbon adsorber (e.g., a purged hydrocarbon adsorber) to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream during an adsorption step (e.g., adsorption step 2600).
  • adsorption step can occur at a first pressure.
  • the light hydrocarbon stream can be characterized by a pressure of from 600 kPa to 3,000 kPa, alternatively from 1,000 kPa to 2,700 kPa, or alternatively from 1,500 kPa to 2,500 kPa.
  • the light hydrocarbon stream can be pressurized (e.g., via one or more compressors) to a pressure of from 600 kPa to 3,000 kPa, alternatively from 1,000 kPa to 2,700 kPa, or alternatively from 1,500 kPa to 2,500 kPa, prior to step 2600 of contacting the light hydrocarbon stream with a purged hydrocarbon adsorber.
  • the light hydrocarbon stream (380 and/or 304) that is emitted from a distillation column (350 and/or 301) can have a pressure that is lower than the first pressure.
  • the light hydrocarbon stream can be optionally pressurized (e.g., via one or more compressors) to the first pressure prior to contacting at least a portion of the light hydrocarbon stream with the hydrocarbon adsorber.
  • the light hydrocarbon stream can be sent to one or more compressors for pressurizing prior to contacting with the hydrocarbon adsorber.
  • an inert gas e.g., a gas or gas mixture that does not adsorb onto the hydrocarbon adsorber; a sweeping gas; a spent sweeping gas; etc.
  • the inert gas can comprise isobutane and/or nitrogen.
  • introducing an inert gas (e.g., a sweeping gas) to the PSA unit during step 2600 along with a light hydrocarbon stream can increase the pressure in the PSA unit to a desired value (e.g., first pressure).
  • the hydrocarbon adsorber can selectively adsorb ethane versus ethylene.
  • the hydrocarbon adsorber is characterized by an adsorption selectivity of ethane versus ethylene as determined by volumetric adsorption at 298 K and at the first pressure of equal to or greater than 2, alternatively greater than 5, alternatively greater than 7, or alternatively greater than 10.
  • the non-adsorbed gas stream 520 can comprise recovered ethylene, e.g., ethylene that was present in the light hydrocarbon stream and was subsequently recovered via the non-adsorbed gas stream.
  • the non-adsorbed gas stream 520 can further comprise small amounts of ethane (e.g., ethane that was not adsorbed by the hydrocarbon adsorber).
  • ethane e.g., ethane that was not adsorbed by the hydrocarbon adsorber.
  • nitrogen and isobutane will not be adsorbed by the hydrocarbon adsorber, and as such the hydrocarbon adsorber is specifically chosen for selectively adsorbing ethane.
  • a small amount of ethylene can be adsorbed by the hydrocarbon adsorber, however, as indicated by the adsorption selectivity of ethane versus ethylene of the hydrocarbon adsorber, the amount of ethylene adsorbed by the hydrocarbon adsorber is much lower than the amount of ethane adsorbed by the hydrocarbon adsorber.
  • recovered ethylene comprises at least a portion of the ethylene of the light hydrocarbon stream.
  • a molar ratio of recovered ethylene to ethylene of the light hydrocarbon stream can be from 0.1 to 1, alternatively from 0.3 to 0.9, or alternatively from 0.4 to 0.8.
  • the PEP process 2000 can generally comprise the step 2700 of contacting the loaded hydrocarbon adsorber with a sweeping gas stream to yield a hydrocarbon adsorber and a recovered adsorbed gas stream.
  • Contacting the loaded hydrocarbon adsorber with a sweeping gas stream can yield a hydrocarbon adsorber (e.g., unloaded hydrocarbon adsorber, regenerated hydrocarbon adsorber, etc.) and a recovered adsorbed gas stream 530, wherein the sweeping gas sweeps away the desorbed ethane.
  • a hydrocarbon adsorber e.g., unloaded hydrocarbon adsorber, regenerated hydrocarbon adsorber, etc.
  • the recovered adsorbed gas stream 530 wherein the sweeping gas sweeps away the desorbed ethane.
  • at least a portion of the recovered adsorbed gas stream comprising desorbed ethane can be recycled to an ethylene production process.
  • a sweeping gas can be used in each of the three steps: adsorption step, desorption step, and/or purging step.
  • a feed stream e.g., light hydrocarbon stream 380, 304
  • a sweeping gas e.g., sweeping gas stream 510
  • the PSA unit e.g., PSA unit 500
  • a sweeping gas e.g., sweeping gas stream 510
  • the adsorption step at least a portion of the components of the sweeping gas can be recovered in the non-adsorbed gas stream along with other non-adsorbed hydrocarbons (e.g., second hydrocarbon, ethylene, etc.), as the sweeping gas components do not adsorb on the hydrocarbon adsorber.
  • the pressure in the PSA unit is lower when compared to the desorption step (e.g., second pressure versus first pressure) and a sweeping gas can be communicated to the PSA unit to push through the adsorbed gases (e.g., adsorbed first hydrocarbon, adsorbed ethane, etc.).
  • the desorption step at least a portion of the components of the sweeping gas can be recovered in the recovered adsorbed gas stream, along with desorbed hydrocarbons (e.g., desorbed first hydrocarbon, desorbed ethane, etc.).
  • a sweeping gas can be communicated to the PSA unit to purge the PSA unit, wherein the sweeping gas provides for an increased pressure within the PSA unit (e.g., first pressure).
  • the desorption step at least a portion of the components of the sweeping gas can be recovered in the spent sweeping gas, wherein a composition of the spent sweeping gas can be about the same as a composition of the sweeping gas.
  • a sweeping gas stream 510 can be communicated to the PSA unit 500 during a desorption step to aid in the recovery of the adsorbed hydrocarbons (e.g., adsorbed ethane).
  • the sweeping gas e.g., isobutane and/or nitrogen
  • the hydrocarbon adsorber bed e.g., open flow channels, spaces between hydrocarbon adsorber particles, hydrocarbon adsorber pores, support pores, etc.
  • desorbed hydrocarbons e.g., desorbed ethane
  • a pressure in the PSA unit can be allowed to decrease during step 2700 of contacting the loaded hydrocarbon adsorber with a sweeping gas stream to the second pressure.
  • the second pressure can be the atmospheric pressure.
  • a pressure of the sweeping gas can be the second pressure (e.g., atmospheric pressure).
  • the atmospheric pressure can be defined as the force per unit area exerted on a surface by the weight of air above that surface in the atmosphere of Earth, and as such the atmospheric pressure can vary depending on where the location is on Earth. Generally, the atmospheric pressure can be considered to have a value of 100-110 kPa.
  • At least a portion of the loaded hydrocarbon adsorber can be contacted with a sweeping gas at a second pressure to yield unloaded hydrocarbon adsorber and desorbed ethane, wherein the desorbed ethane comprises at least a portion of the adsorbed ethane.
  • a sweeping gas at least a portion of any other hydrocarbons (e.g., ethylene) that were adsorbed in small amounts along with the ethane by the hydrocarbon adsorber will also be desorbed during desorption step 2700, and will be swept by the sweeping gas along with the desorbed ethane.
  • the hydrocarbon adsorbers optionally can be calcined (e.g., heated to high temperatures, for example greater than 300 °C) to remove residual adsorbed hydrocarbons and then returned into the PEP process.
  • the recovered adsorbed gas stream 530 comprises sweeping gas and recovered ethane, wherein the recovered ethane comprises at least a portion of the desorbed ethane.
  • the recovered adsorbed gas stream primarily contains a sweeping gas and ethane.
  • the desorbed ethane comprises at least a portion of the adsorbed ethane. In an example, the adsorbed ethane comprises at least a portion of the ethane of the light hydrocarbon stream. In an example, the desorbed ethane comprises at least a portion of the ethane of the light hydrocarbon stream. In an example, a molar ratio of desorbed ethane to ethane of the light hydrocarbon stream can be from 0.1 to 1, alternatively from 0.3 to 0.9, or alternatively from 0.4 to 0.8.
  • the PEP process 2000 can generally comprise the step 2800 of contacting the hydrocarbon adsorber with the sweeping gas stream to yield the purged hydrocarbon adsorber and a spent sweeping gas.
  • the purging step 2800 could also be referred to as a "priming step” or a "pressurizing step.”
  • purging step 2800, along with desorption step 2700, contributes to the regeneration of the hydrocarbon adsorption bed for use in a subsequent adsorption step 2600 of a PSA process.
  • the spent sweeping gas comprises a sweeping gas and residual hydrocarbons, wherein the residual hydrocarbons comprise at least a portion of any hydrocarbons that were not removed by the sweeping gas during step 2700 of contacting the loaded hydrocarbon adsorber with a sweeping gas stream.
  • the residual hydrocarbons comprise ethane, ethylene, or combinations thereof.
  • step 2800 of contacting the hydrocarbon adsorber with the sweeping gas stream occurs at the first pressure.
  • the sweeping gas utilized in step 2700 of contacting the loaded hydrocarbon adsorber with a sweeping gas stream has a pressure of about the second pressure.
  • the sweeping gas can be pressurized (e.g., via one or more compressors) to about the first pressure prior to step 2800 of contacting the hydrocarbon adsorber with the sweeping gas stream.
  • the sweeping gas stream can be sent to one or more compressors for pressurizing prior to contacting with the hydrocarbon adsorber in step 2800.
  • the sweeping gas e.g., isobutane and/or nitrogen
  • the hydrocarbon adsorber bed e.g., open flow channels, spaces between hydrocarbon adsorber particles, hydrocarbon adsorber pores, support pores, etc.
  • the sweeping gas ensures that the pressure in the entire hydrocarbon adsorber bed is about the first pressure.
  • the spent sweeping gas comprises residual hydrocarbons in an amount of less than 10 wt.%, alternatively less than 9 wt.%, alternatively less than 8 wt.%, alternatively less than 7 wt.%, alternatively less than 6 wt.%, alternatively less than 5 wt.%, alternatively less than 4 wt.%, alternatively less than 3 wt.%, alternatively less than 2 wt.%, alternatively less than 1 wt.%, based on the total weight of the spent sweeping gas.
  • the spent sweeping gas can be emitted from the PSA unit 500 during the purging step 2800; the recovered adsorbed gas stream 530 can be emitted from the PSA unit 500 during the desorption step 2700; and the non-adsorbed gas stream 520 can be emitted from the PSA unit 500 during the adsorption step 2600.
  • the recovered adsorbed gas stream 530 and/or the spent sweeping gas can be sent to flare.
  • At least a portion of the spent sweeping gas can be recycled to the sweeping gas stream, such as for example to a sweeping gas stream utilized in purging step 2800, to a sweeping gas stream utilized in desorption step 2700, to a sweeping gas stream utilized in adsorption step 2600, etc.
  • the spent sweeping gas can be contacted with at least a portion of the light hydrocarbon stream during step 2600 of contacting the light hydrocarbon stream with a purged hydrocarbon adsorber.
  • the spent sweeping gas can be combined with a sweeping gas stream prior to step 2600 of contacting the light hydrocarbon stream with a purged hydrocarbon adsorber.
  • a process for component separation in a polymer production system comprising selectively separating a first hydrocarbon (e.g., by-product hydrocarbon, by-product ethane) from a second hydrocarbon (e.g., unreacted monomer, unreacted ethylene)
  • a cyclic or loop process e.g., PSA cyclic process
  • the cyclic process can comprise three steps: an adsorption step 2600, a desorption step 2700, and a purging step 2800.
  • purging step 2800 of contacting the hydrocarbon adsorber with the sweeping gas stream is the priming step that a hydrocarbon adsorber bed has to undergo, prior to cycling through an adsorption step, a desorption step, and a purging step. Further, as will be appreciated by one of skill in the art, and with the help of this disclosure, purging step 2800 "primes" the hydrocarbon adsorber for entering a PSA cyclic process for component separation.
  • adsorption step necessitates a purged hydrocarbon adsorber, thereby the hydrocarbon adsorber beds have to be purged or primed (e.g., undergo purging step 2800) prior to entering the PSA cycles comprising an adsorption step, a desorption step, and a purging step.
  • deciding when a step e.g., adsorption step, desorption step, purging step
  • a step can be achieved by in-line or real-time monitoring of effluent gas streams.
  • in-line monitoring can be achieved by using any suitable analytical tools and methodology, e.g., gas chromatography, mass spectrometry, flame ionization detector, and the like, or combinations thereof.
  • the non-adsorbed gas stream can be monitored, and an increase in ethane content of the non-adsorbed gas stream could signal that it is time to cycle the PSA unit to the desorption step.
  • the recovered adsorbed gas stream can be monitored, and a decrease in ethane content of the recovered adsorbed gas stream could signal that it is time to cycle the PSA unit to the purging step.
  • a PSA unit comprises at least one hydrocarbon adsorber bed disposed therein.
  • a PSA unit comprises a plurality of hydrocarbon adsorber beds disposed therein. While the PSA units will be discussed in detail in the context of two and/or three PSA units operating in parallel, it should be understood that any suitable number of PSA units can be used for processing a gas stream (e.g., light hydrocarbon stream, gaseous mixture, hydrocarbon mixture, etc.), such as for example one, two, three, four, five, six, seven, eight, nine, ten, or more PSA units.
  • a gas stream e.g., light hydrocarbon stream, gaseous mixture, hydrocarbon mixture, etc.
  • a PSA system can comprise from 2 to 8 pressure swing adsorption units operated in parallel, alternatively from 3 to 7 pressure swing adsorption units operated in parallel, or alternatively from 4 to 6 pressure swing adsorption units operated in parallel.
  • the PSA unit 500 as shown in Figure 1A and/or Figure 1B comprises at least two PSA units working in parallel.
  • PSA system 501 generally comprises two PSA units operating in parallel.
  • PSA system 501 generally comprises a first PSA unit 505 and a second PSA unit 506.
  • the first PSA unit 505 and the second PSA unit 506 can operate concurrently or simultaneously.
  • the adsorption step 2600 (e.g., contacting the light hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream) can occur in the first PSA unit 505 at the first pressure and the desorption step 2700 (e.g., contacting the loaded hydrocarbon adsorber with a sweeping gas stream to yield a hydrocarbon adsorber and a recovered adsorbed gas stream) can occur in the second PSA unit 506 at the second pressure, wherein the first PSA unit and the second PSA unit are operated in parallel.
  • the purging step 2800 (e.g., contacting the hydrocarbon adsorber with the sweeping gas stream to yield the purged hydrocarbon adsorber and a spent sweeping gas) can occur in the second PSA unit at the first pressure, subsequent to the desorption step 2700.
  • the purging step 2800 can occur in the second PSA unit while the first PSA unit is still undergoing the adsorption step 2600.
  • the purging step 2800 can occur in the second PSA unit while the first PSA unit is undergoing a desorption step 2700 subsequent to the adsorption step 2600.
  • the first PSA system 501 can comprise a first PSA unit 505 and a second PSA unit 506, wherein the first PSA unit 505 is undergoing desorption step 2700 (subsequent to adsorption step 2600) and wherein the second PSA unit 506 is undergoing adsorption step 2600 (subsequent to desorption step 2700 and purging step 2800).
  • each PSA unit will successively cycle through each of the cycling steps: an adsorption step, a desorption step, and a purging step, wherein the PSA units are offset such that at any given time one of the units is ready to or undergoing the adsorption step, thereby providing for a continuous process.
  • a light hydrocarbon stream 381 (e.g., light hydrocarbon stream 380 in Figure 1A and/or light hydrocarbon stream 304 Figure 1B ) can be communicated to a first PSA unit 505 operating at the first pressure.
  • a sweeping gas stream 511 can be communicated to the first PSA unit 505 during the adsorption step 2600.
  • a non-adsorbed gas stream 521 (e.g., non-adsorbed gas stream 520 in Figure 1A and/or Figure 1B ) can be communicated from the first PSA unit 505 to the INRU 601 (e.g., INRU 600 in Figure 1A and/or Figure 1B ).
  • a gas stream 611 (e.g., gas stream 610 in Figure 1A and/or Figure 1B ) comprising nitrogen 602 (e.g., nitrogen 615 in Figure 1A and/or Figure 1B ) can be emitted from the INRU 601. At least a portion of the nitrogen 602 can be recycled 604 to the first PSA unit 505, for example via the sweeping gas stream 511 (e.g., sweeping gas stream 510 in Figure 1A and/or Figure 1B ), and/or recycled 605 to the second PSA unit 506, for example via the sweeping gas stream 512 (e.g., sweeping gas stream 510 in Figure 1A and/or Figure 1B ).
  • the sweeping gas stream 511 e.g., sweeping gas stream 510 in Figure 1A and/or Figure 1B
  • the second PSA unit 506 for example via the sweeping gas stream 512 (e.g., sweeping gas stream 510 in Figure 1A and/or Figure 1B ).
  • a gas stream (e.g., gas stream 620 in Figure 1A and/or Figure 1B ) comprising isobutane and ethylene (e.g., isobutane and ethylene 625 in Figure 1A and/or Figure 1B ) can be emitted from the INRU 601.
  • gas stream 620 in Figure 1A and/or Figure 1B comprising isobutane and ethylene (e.g., isobutane and ethylene 625 in Figure 1A and/or Figure 1B ) can be emitted from the INRU 601.
  • a sweeping gas stream 511 can be communicated to the first PSA unit 505, and recovered adsorbed gas stream 531 (e.g., recovered adsorbed gas stream 530 in Figure 1A and/or Figure 1B ) can be emitted from the first PSA unit 505.
  • recovered adsorbed gas stream 531 e.g., recovered adsorbed gas stream 530 in Figure 1A and/or Figure 1B
  • a sweeping gas stream 512 can be communicated to a second PSA unit 506 operating at the second pressure.
  • a recovered adsorbed gas stream 532 e.g., recovered adsorbed gas stream 530 in Figure 1A and/or Figure 1B
  • a light hydrocarbon stream 382 e.g., light hydrocarbon stream 380 in Figure 1A and/or light hydrocarbon stream 304 Figure 1B
  • non-adsorbed gas stream 522 e.g., non-adsorbed gas stream 520 in Figure 1A and/or Figure 1B
  • the PSA unit 500 as shown in Figure 1A and/or Figure 1B comprises at least three PSA units working in parallel.
  • a second PSA system 502 which has a number of system components common with PSA system 501.
  • the second PSA system 502 comprises three PSA units operating in parallel (as opposed two PSA units operating in parallel of PSA system 501).
  • PSA system 502 generally comprises a first PSA unit 505, a second PSA unit 506, and a third PSA unit 507.
  • the first PSA unit 505, the second PSA unit 506, and the third PSA unit 507 can operate concurrently or simultaneously.
  • the adsorption step 2600 can occur in the first PSA unit 505 at the first pressure; the desorption step 2700 can occur in the second PSA unit 506 at the second pressure; and the purging step 2800 (e.g., contacting the hydrocarbon adsorber with the sweeping gas stream to yield the purged hydrocarbon adsorber and a spent sweeping gas) can occur in a third PSA unit 507 at the first pressure; wherein the first PSA unit, the second PSA unit, and the third PSA unit are operated in parallel, and wherein the first pressure is greater than the second pressure.
  • the purging step 2800 e.g., contacting the hydrocarbon adsorber with the sweeping gas stream to yield the purged hydrocarbon adsorber and a spent sweeping gas
  • the second PSA system 502 can comprise a first PSA unit 505, a second PSA unit 506, and a third PSA unit 507, wherein the first PSA unit 505 is undergoing desorption step 2700 (subsequent to adsorption step 2600), wherein the second PSA unit 506 is undergoing purging step 2800 (subsequent to desorption step 2700), and wherein the third PSA unit 507 is undergoing adsorption step 2600 (subsequent to purging step 2800).
  • the second PSA system 502 can comprise a first PSA unit 505, a second PSA unit 506, and a third PSA unit 507, wherein the first PSA unit 505 is undergoing purging step 2800 (subsequent to desorption step 2700), wherein the second PSA unit 506 is undergoing adsorption step 2600 (subsequent to purging step 2800), and wherein the third PSA unit 507 is undergoing desorption step 2700 (subsequent to adsorption step 2600).
  • each PSA unit will successively cycle through each of the cycling steps: an adsorption step, a desorption step, and a purging step, wherein the PSA units are offset such that at any given time one of the units is ready to or undergoing the adsorption step, thereby providing for a continuous process.
  • a sweeping gas stream 513 (e.g., sweeping gas stream 510 in Figure 1A and/or Figure 1B ) can be communicated to the third PSA unit 507 operating at the first pressure.
  • a spent sweeping gas 540 can be emitted from the third PSA unit 507 during the purging step 2800. At least a portion of the spent sweeping gas 540 can be recycled 541 to the first PSA unit and/or recycled 542 the second PSA unit, such as for example via the sweeping gas stream 511 and/or the sweeping gas stream 512, respectively.
  • a light hydrocarbon stream 383 (e.g., light hydrocarbon stream 380 in Figure 1A and/or light hydrocarbon stream 304 Figure 1B ) can be communicated to the third PSA unit 507, and non-adsorbed gas stream 523 (e.g., non-adsorbed gas stream 520 in Figure 1A and/or Figure 1B ) can be communicated from the third PSA unit 507 and to the INRU 601.
  • at least a portion of the nitrogen 602 can be recycled 606 to the third PSA unit 507, for example via the sweeping gas stream 513 (e.g., sweeping gas stream 510 in Figure 1A and/or Figure 1B ).
  • the sweeping gas stream 513 can be communicated to the third PSA unit 507, and a recovered adsorbed gas stream 533 (e.g., recovered adsorbed gas stream 530 in Figure 1A and/or Figure 1B ) can be emitted from the third PSA unit 507.
  • a recovered adsorbed gas stream 533 e.g., recovered adsorbed gas stream 530 in Figure 1A and/or Figure 1B
  • the PEP process 2000 can generally comprise the step 2900 of separating the non-adsorbed gas stream into a nitrogen stream and an isobutane and ethylene stream.
  • a non-adsorbed gas stream 520 can be communicated from the PSA unit 500 to the INRU 600. Separating the non-adsorbed gas stream 520 into a nitrogen stream 610 and an isobutane and ethylene stream 620 comprising isobutane and ethylene 625 can be accomplished in the INRU 600.
  • INRU 600 can comprise a membrane recovery unit, a pressure swing adsorption unit, a refrigeration unit, and the like.
  • the INRU 600 can separate the non-adsorbed gas stream into the nitrogen stream 610 and the isobutane and ethylene stream 620.
  • At least a portion of the nitrogen stream 610 can be recycled 616 to the purge column 400, for example via the purge gas stream 410. In an example, at least a portion of the nitrogen stream 610 can be recycled 617 to the PSA unit 500, for example via the sweeping gas stream 510. Moreover, fresh nitrogen can be added to a nitrogen circuit comprising the purge gas stream 410 and/or a PSA unit 500 to account for nitrogen losses in the purge column 400, in the PSA unit 500 and/or in the INRU 600.
  • At least a portion of the isobutane and ethylene 625 comprising ethylene can be pressurized (e.g., via one or more compressors) and re-introduced 626 (e.g., as shown in Figure 1A and/or Figure 1B ) into a PEP process (e.g., into the slurry loop reactor system 100), for example via the reagents stream 110.
  • a reintroduction stream 626 can be communicated to the purifier 102.
  • at least a portion of the isobutane and ethylene 625 comprising ethylene can be optionally cooled in a heat exchanger and collected in a recycle surge tank for feed to a reactor (e.g., reactor 104, reactor 106).
  • a skilled artisan will recognize that industrial and commercial polyethylene manufacturing processes can necessitate one or more, often several, compressors or similar apparatuses. Such compressors are used throughout polyethylene manufacturing, for example to pressurize reactors 104, 106 during polymerization. Further, a skilled artisan will recognize that a polyethylene manufacturing process includes one or more deoxygenators and/or similar deoxidizing apparatuses, for instance for purifying solvents or reactants and/or for purging reactors of oxygen.
  • compressors, deoxygenators, and various other components are already employed in various polyethylene processes and systems, the opportunity for increased operation of such apparatuses can improve the overall efficiency of polyethylene production systems and processes. For example, when a portion of a PEP process or system is taken off-line for maintenance and/or repair, other portions of the system (e.g., a compressor, a deoxygenator, a reactor, etc.) can continue to provide service according to the current processes. Operating and/or reallocating resources for operation of the disclosed PEP systems and/or processes can thereby increase the efficiency with which conventional systems are used.
  • a process for component (e.g., hydrocarbon) separation in a polymer production system can comprise the steps of (a) separating a polymerization product stream into a gas stream and a polymer stream; (b) processing the gas stream in one or more distillation columns to yield a light hydrocarbon stream, wherein the light hydrocarbon stream comprises ethylene and ethane; (c) contacting at least a portion of the light hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein at least a portion of the ethane is adsorbed by the purged hydrocarbon adsorber at a pressure of 2,200 kPa to yield adsorbed ethane, wherein the non-adsorbed gas stream comprises recovered ethylene, wherein the recovered ethylene comprises at least a portion of the ethylene of the light hydrocarbon stream, wherein the light hydrocarbon stream is characterized by a temperature of -25
  • a process for hydrocarbon recovery can comprise the steps of (a) providing a hydrocarbon stream comprising a first hydrocarbon and a second hydrocarbon, wherein the first hydrocarbon is a saturated hydrocarbon, and wherein the second hydrocarbon is an olefin; (b) contacting at least a portion of the hydrocarbon stream with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein at least a portion of the first hydrocarbon is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed first hydrocarbon, and wherein the non-adsorbed gas stream comprises recovered second hydrocarbon, wherein the recovered second hydrocarbon comprises at least a portion of the second hydrocarbon of the hydrocarbon stream, wherein the hydrocarbon adsorber is characterized by an adsorption selectivity of the first hydrocarbon versus the second hydrocarbon as determined by volumetric adsorption at 298 K and at the first pressure of equal to or greater than 2; (c)
  • a pressure swing adsorption system can comprise at least two pressure swing adsorption units, wherein the adsorption step, the desorption step, and the purging step are offset (do not occur simultaneously within the same PSA unit) between the at least two pressure swing adsorption units; wherein the at least two pressure swing adsorption units are operated in parallel; wherein the pressure swing adsorption unit comprises at least one hydrocarbon adsorber bed disposed therein; wherein the hydrocarbon adsorber bed comprises a hydrocarbon adsorber; wherein the hydrocarbon adsorber is contacted with a sweeping gas stream to yield a purged hydrocarbon adsorber; wherein the pressure swing adsorption unit adsorbs at a first pressure, wherein the purged hydrocarbon adsorber adsorbs a first hydrocarbon to yield a loaded hydrocarbon adsorber comprising an adsorbed first hydrocarbon and a non-adsorbed gas stream comprising a second hydrocarbon; wherein the hydrocarbon adsorber has an ad
  • One or more of the disclosed systems can advantageously display improvements in one or more system and/or process characteristics when compared to otherwise similar systems and/or processes lacking a step of ethylene recovery in a PSA unit.
  • the PSA unit as disclosed herein can advantageously allow for the recovery of a substantial portion of ethylene that would otherwise be lost due to conventional operation of such systems or processes, for example, by flaring.
  • One or more of the disclosed systems can allow for the recovery of up to 75%, alternatively, up to 85%, alternatively, up to 90%, alternatively, up to 95% by total weight of ethylene from a light hydrocarbon stream that would otherwise be lost.
  • the recovery of such a portion of ethylene e.g., unreacted ethylene monomers
  • can yield a significant economic benefit for example, by improving the efficiency of usage of ethylene and decreasing capital inputs associated with the acquisition of ethylene.
  • the PSA unit as disclosed herein can advantageously decrease the amount of ethane that is returned to a polymerization reactor (such as reactors 104 and/or 106) via a recycle stream (e.g., stream 626).
  • a polymerization reactor such as reactors 104 and/or 106
  • a recycle stream e.g., stream 626
  • the overall efficiency of the polyethylene production can be improved (for example, by increasing the ethylene concentration without reaching a bubble point in the loop reactor).
  • decreasing the amount of ethane in a stream can improve polymerization reactor efficiency, improve catalyst efficiency, reduce polymer fouling, reduce polymerization downtime, improve production of bimodal polymer types, improve production of copolymers, or combinations thereof.
  • the PSA unit as disclosed herein can advantageously reduce a load on a compressor of the INRU due to a reduced gas stream throughput through such compressor.
  • the INRU comprises a pressure swing adsorption bed
  • such bed can advantageously display an increased capacity for isobutane adsorption, owing to the decreased content of ethane in the gas stream entering the INRU.
  • the INRU comprises a membrane recovery unit
  • such membrane can advantageously display an increased throughput of isobutane, owing to the decreased content of ethane in the gas stream entering the INRU. Additional advantages of the systems and/or processes for the production of a polyethylene polymer as disclosed herein can be apparent to one of skill in the art viewing this disclosure.
  • a first disclosure which is a process for component separation in a polymer production system, the process comprising:
  • a second disclosure which is the process of the first disclosure, wherein the hydrocarbon adsorber is characterized by an adsorption selectivity of ethane versus ethylene as determined by volumetric adsorption at 298 K and at the first pressure of equal to or greater than 2.
  • a third disclosure which is the process of any of the first through the second disclosures, wherein the first pressure is greater than the second pressure by equal to or greater than 400 kPa.
  • a fourth disclosure which is the process of any of the first through the third disclosures, wherein the first pressure is from 600 kPa to 3,000 kPa.
  • a fifth disclosure which is the process of any of the first through the fourth disclosures, wherein (c) contacting the light hydrocarbon stream with the purged hydrocarbon adsorber, (d) contacting the loaded hydrocarbon adsorber with the sweeping gas stream, and (e) contacting the unloaded hydrocarbon adsorber with the sweeping gas stream occur at a temperature of from - 30 °C to 50 °C.
  • a sixth disclosure which is the process of any of the first through the fifth disclosures, wherein the light hydrocarbon stream obtained by (b) processing the gas stream has a pressure of from 600 kPa to 3,000 kPa.
  • a seventh disclosure which is the process of any of the first through the sixth disclosures, wherein the light hydrocarbon stream obtained by (b) processing the gas stream is further pressurized to a pressure of from 600 kPa to 3,000 kPa prior to (c) contacting with the purged hydrocarbon adsorber.
  • An eighth disclosure which is the process of any of the first through the seventh disclosures, wherein a molar ratio of desorbed ethane to ethane of the light hydrocarbon stream is from 0.1 to 1.
  • a ninth disclosure which is the process of any of the first through the eighth disclosures, wherein a molar ratio of recovered ethylene to ethylene of the light hydrocarbon stream is from 0.1 to 1.
  • a tenth disclosure which is the process of any of the first through the ninth disclosures, wherein at least a portion of the sweeping gas stream and/or at least a portion of the spent sweeping gas is contacted with at least a portion of the light hydrocarbon stream during (c) contacting with the purged hydrocarbon adsorber.
  • An eleventh disclosure which is the process of any of the first through the tenth disclosures, wherein the sweeping gas stream comprises isobutane and/or nitrogen.
  • a twelfth disclosure which is the process of any of the first through the eleventh disclosures, wherein at least a portion of the non-adsorbed gas stream is separated into a nitrogen stream and an isobutane and ethylene stream.
  • a thirteenth disclosure which is the process of the twelfth disclosure, wherein at least a portion of the isobutane and ethylene stream is recycled as a reagent for the polymer production system.
  • a fourteenth disclosure which is the process of any of the twelfth through the thirteenth disclosures, wherein at least a portion of the nitrogen stream is recycled to the sweeping gas stream.
  • a fifteenth disclosure which is the process of any of the twelfth through the fourteenth disclosures, wherein at least a portion of the nitrogen stream is recycled to a purge gas stream contacting at least a portion of the polymer stream.
  • a sixteenth disclosure which is the process of any of the first through the fifteenth disclosures, wherein at least a portion of the gas stream is distilled into a light distillation bottoms stream comprising olefin-free isobutane, wherein at least a portion of the light distillation bottoms stream is recycled to the sweeping gas stream.
  • a seventeenth disclosure which is the process of any of the first through the sixteenth disclosures, wherein at least a portion of the spent sweeping gas is recycled to the sweeping gas stream.
  • An eighteenth disclosure which is the process of any of the first through the seventeenth disclosures, wherein at least a portion of the recovered adsorbed gas stream is recycled to an ethylene production process.
  • a nineteenth disclosure which is the process of any of the first through the eighteenth disclosures, wherein the hydrocarbon adsorber is part of a pressure swing adsorption unit.
  • a twentieth disclosure which is the process of any of the first through the nineteenth disclosures, wherein (c) contacting the light hydrocarbon stream with the purged hydrocarbon adsorber occurs in a pressure swing adsorption unit.
  • a twenty-first disclosure which is the process of the nineteenth disclosure, wherein the pressure swing adsorption unit is characterized by a cycle time of from 10 seconds to 1 hour.
  • a twenty-second disclosure which is the process of any of the nineteenth through the twenty-first disclosures, wherein from 2 to 8 pressure swing adsorption units are operated in parallel.
  • a twenty-third disclosure which is the process of any of the first through the twenty-second disclosures, wherein (c) contacting the light hydrocarbon stream with the purged hydrocarbon adsorber occurs in a first pressure swing adsorption unit and (d) contacting the loaded hydrocarbon adsorber with the sweeping gas stream and (e) contacting the unloaded hydrocarbon adsorber with the sweeping gas stream occur in a second pressure swing adsorption unit, wherein the first pressure swing adsorption unit and the second pressure swing adsorption unit are operated in parallel.
  • a twenty-fourth disclosure which is the process of any of the first through the twenty-third disclosures, wherein (c) contacting the light hydrocarbon stream with the purged hydrocarbon adsorber occurs in a first pressure swing adsorption unit; (d) contacting the loaded hydrocarbon adsorber with the sweeping gas stream occurs in a second pressure swing adsorption unit; and (e) contacting the unloaded hydrocarbon adsorber with the sweeping gas stream occur in a third pressure swing adsorption unit, wherein the first pressure swing adsorption unit, the second pressure swing adsorption unit and the third pressure swing adsorption unit are operated in parallel.
  • a twenty-fifth disclosure which is the process of any of the first through the twenty-fourth disclosures, wherein the hydrocarbon adsorber comprises a zeolitic imidazolate framework (ZIF).
  • ZIF zeolitic imidazolate framework
  • a twenty-sixth disclosure which is the process of the twenty-fifth disclosure, wherein the zeolitic imidazolate framework is characterized by a pore window size of from 0.2 nm to 0.5 nm.
  • a twenty-seventh disclosure which is the process of any of the twenty-fifth through the twenty-sixth disclosures, wherein the zeolitic imidazolate framework comprises ZIF-7, ZIF-8, ZIF-65, ZIF-67, or combinations thereof.
  • a twenty-eighth disclosure which is the process of any of the first through the twenty-seventh disclosures, wherein the hydrocarbon adsorber is in the form of particles, pellets, beads, hollow beads, spheres, ovals, fibers, hollow fibers, tubes, hollow tubes, rods, platelets, disks, plates, ribbons, or combinations thereof.
  • a twenty-ninth disclosure which is the process of any of the first through the twenty-eighth disclosures, wherein the hydrocarbon adsorber is characterized by a particle size of from 0.1 mm to 5 mm.
  • a thirtieth disclosure which is the process of any of the first through the twenty-ninth disclosures, wherein the hydrocarbon adsorber further comprises a support.
  • a thirty-first disclosure which is the process of the thirtieth disclosure, wherein the zeolitic imidazolate framework contacts at least a portion of the support, is distributed throughout the support, or combinations thereof.
  • a thirty-second disclosure which is the process of any of the thirtieth through the thirty-first disclosures, wherein the support has a porosity of from 0 vol.% to 99 vol.% based on the total volume of the support.
  • a thirty-third disclosure which is the process of any of the thirtieth through the thirty-second disclosures, wherein the support comprises a support outer surface, wherein at least a portion of the support outer surface is in contact with the zeolitic imidazolate framework.
  • a thirty-fourth disclosure which is a process for component separation in a polymer production system, the process comprising:
  • a thirty-fifth disclosure which is a process for component separation in a polymer production system, the process comprising:
  • a thirty-sixth disclosure which is a process for hydrocarbon recovery, the process comprising:
  • a thirty-seventh disclosure which is a pressure swing adsorption system comprising at least two pressure swing adsorption units; wherein the at least two pressure swing adsorption units are operated in parallel; wherein the pressure swing adsorption unit comprises at least one hydrocarbon adsorber bed disposed therein; wherein the hydrocarbon adsorber bed comprises a hydrocarbon adsorber; wherein the hydrocarbon adsorber is contacted with a sweeping gas stream to yield a purged hydrocarbon adsorber; wherein the pressure swing adsorption unit adsorbs at a first pressure, wherein the purged hydrocarbon adsorber adsorbs a first hydrocarbon to yield a loaded hydrocarbon adsorber comprising an adsorbed first hydrocarbon and a non-adsorbed gas stream comprising a second hydrocarbon; wherein the hydrocarbon adsorber has an adsorption selectivity of the first hydrocarbon versus the second hydrocarbon as determined by volumetric adsorption at 298 K and at the first pressure of equal to or greater
  • a thirty-eighth disclosure which is the pressure swing adsorption system of the thirty-seventh disclosure, wherein the hydrocarbon adsorber bed has a bed thickness of from 0.1 ft to 20 ft.
  • a thirty-ninth disclosure which is a process for ethylene polymerization, the process comprising:
  • a fortieth disclosure which is the process of the thirty-ninth disclosure, wherein at least a portion of the sweeping gas stream and/or at least a portion of the spent sweeping gas is contacted with at least a portion of the light hydrocarbon stream during (d) contacting with the purged hydrocarbon adsorber; wherein at least a portion of the non-adsorbed gas stream is separated into a nitrogen stream and an isobutane and ethylene stream; wherein at least a portion of the isobutane and ethylene stream is recycled as a reagent for (a) polymerizing ethylene; wherein at least a portion of the nitrogen stream is recycled to the sweeping gas stream; wherein at least a portion of the nitrogen stream is recycled to a purge gas stream contacting at least a portion of the polymer stream; wherein at least a portion of the gas stream is distilled into a light distillation bottoms stream comprising olefin-free isobutane, wherein at least a portion of the light distill
  • a forty-first disclosure which is a process for hydrocarbon recovery, the process comprising:

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Supply & Treatment (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation Of Gases By Adsorption (AREA)

Claims (15)

  1. Procédé de séparation de composants dans un système de production de polymère, le procédé comprenant :
    (a) la séparation d'un flux de produit de polymérisation en un flux gazeux et un flux de polymère ;
    (b) le traitement du flux gazeux dans une ou plusieurs colonnes de distillation pour donner un flux d'hydrocarbures légers, le flux d'hydrocarbures légers comprenant de l'éthylène et de l'éthane ;
    (c) la mise en contact d'au moins une partie du flux d'hydrocarbures légers avec un adsorbeur d'hydrocarbures purgés pour donner un adsorbeur d'hydrocarbures chargés et un flux gazeux non adsorbé, au moins une partie de l'éthane étant sélectivement adsorbée par l'adsorbeur d'hydrocarbures purgés à une première pression pour donner de l'éthane adsorbé, et le flux gazeux non adsorbé comprenant de l'éthylène récupéré, l'éthylène récupéré comprenant au moins une partie de l'éthylène du flux d'hydrocarbures légers, l'adsorbeur d'hydrocarbures comprenant une structure d'imidazolate zéolithique (ZIF);
    (d) la mise en contact d'au moins une partie de l'adsorbeur d'hydrocarbures chargés avec un flux gazeux de balayage à une seconde pression pour produire un adsorbeur d'hydrocarbures déchargés et un flux gazeux adsorbé récupéré, le flux de gaz adsorbé récupéré comprenant au moins une partie du flux gazeux de balayage et au moins une partie d'éthane désorbé, et l'éthane désorbé comprenant au moins une partie de l'éthane adsorbé, la première pression étant supérieure à la seconde pression égale ou supérieure à 400 kPa ; et
    (e) la mise en contact d'au moins une partie de l'adsorbeur d'hydrocarbures déchargés avec au moins une partie du flux gazeux de balayage à la première pression pour donner l'adsorbeur d'hydrocarbures purgés et un gaz de balayage épuisé.
  2. Procédé selon la revendication 1, la première pression étant de 600 kPa à 3 000 kPa.
  3. Procédé selon la revendication 1 ou la revendication 2, (c) la mise en contact du flux d'hydrocarbures légers avec l'adsorbeur d'hydrocarbures purgés, (d) la mise en contact de l'adsorbeur d'hydrocarbures chargés avec le flux gazeux de balayage, et (e) la mise en contact de l'adsorbeur d'hydrocarbures déchargés avec le flux gazeux de balayage se produisant à une température de -30 °C à 50 °C.
  4. Procédé selon l'une quelconque des revendications précédentes, (c) la mise en contact du flux d'hydrocarbures légers avec l'adsorbeur d'hydrocarbures purgés se produisant dans une première unité d'adsorption modulée en pression ; (d) la mise en contact de l'adsorbeur d'hydrocarbures chargés avec le flux gazeux de balayage se produisant dans une deuxième unité d'adsorption modulée en pression ; et (e) la mise en contact de l'adsorbeur d'hydrocarbures déchargés avec le flux gazeux de balayage se produisant dans une troisième unité d'adsorption modulée en pression, la première unité d'adsorption modulée en pression, la deuxième unité d'adsorption modulée en pression et la troisième unité d'adsorption modulée en pression fonctionnant en parallèle.
  5. Procédé selon l'une quelconque des revendications précédentes, le flux d'hydrocarbures légers obtenu par (b) traitement du flux gazeux ayant une pression de 600 kPa à 3 000 kPa, ou le flux gazeux de balayage comprenant de l'isobutane et/ou de l'azote.
  6. Procédé selon l'une quelconque des revendications précédentes, un rapport molaire de l'éthane désorbé à l'éthane du flux d'hydrocarbures légers étant de 0,1 à 1, ou un rapport molaire de l'éthylène récupéré à l'éthylène du flux d'hydrocarbures légers étant de 0,1 à 1.
  7. Procédé selon l'une quelconque des revendications précédentes, l'adsorbeur d'hydrocarbures faisant partie d'une unité d'adsorption modulée en pression.
  8. Procédé selon l'une quelconque des revendications précédentes, (c) la mise en contact du flux d'hydrocarbures légers avec l'adsorbeur d'hydrocarbures purgés se produisant dans une unité d'adsorption modulée en pression.
  9. Procédé selon la revendication 7, l'unité d'adsorption à variation de pression étant caractérisée par un temps de cycle de 10 secondes à 1 heure, ou de 2 à 8 unités d'adsorption à variation de pression fonctionnant en parallèle.
  10. Procédé selon l'une quelconque des revendications précédentes, la structure d'imidazolate zéolithique comprenant Zn, Co, Ni, Fe, Cu, Mg ou des combinaisons de ceux-ci.
  11. Procédé selon l'une quelconque des revendications précédentes, la structure d'imidazolate zéolithique étant caractérisée par une taille de fenêtre de pore de 0,2 nm à 0,5 nm, ou la structure d'imidazolate zéolithique comprenant ZIF-7, ZIF-8, ZIF-65, ZIF-67, ou des combinaisons de ceux-ci.
  12. Procédé selon l'une quelconque des revendications précédentes, l'adsorbeur d'hydrocarbures ayant la forme de particules, pastilles, perles, billes creuses, sphères, ovales, fibres, fibres creuses, tubes, tubes creux, tiges, plaquettes, disques, plaques, rubans, ou des combinaisons de ceux-ci, ou l'adsorbeur d'hydrocarbures étant caractérisé par une taille de particule de 0,1 mm à 5 mm, ou l'adsorbeur d'hydrocarbures comprenant en outre un support, et la structure d'imidazolate zéolithique entrant en contact avec au moins une partie du support, étant répartie dans l'ensemble du support ou des combinaisons de ceux-ci.
  13. Procédé selon la revendication 1, la première pression étant une pression de 1 000 kPa à 2 700 kPa, le flux d'hydrocarbures légers dans l'étape (c) étant caractérisé par une température de -25 °C à 30 °C, l'adsorbeur d'hydrocarbures étant caractérisé par une sélectivité d'adsorption d'éthane par rapport à l'éthylène telle que déterminée par adsorption volumétrique à 298 K et à une pression de 1 000 kPa à 2 700 kPa égale ou supérieure à 2, l'adsorbeur d'hydrocarbures à l'étape (c) comprenant une structure d'imidazolate zéolithique (ZIF) choisie parmi ZIF-7, ZIF-8 ou à la fois ZIF-7 et ZIF-8 ; la seconde pression étant une pression de 50 kPa à 150 kPa, et le flux gazeux de balayage dans l'étape (d) comprenant de l'isobutane et/ou de l'azote.
  14. Procédé de polymérisation d'éthylène, le procédé comprenant :
    (a) la polymérisation d'éthylène dans un système de réacteur en boucle à combustible en suspension pour obtenir un flux de produit de polymérisation ;
    (b) la séparation d'un flux de produit de polymérisation dans une chambre d'expansion en un flux gazeux et un flux de polymère ;
    (c) le traitement du flux gazeux dans une ou plusieurs colonnes de distillation pour donner un flux d'hydrocarbures légers, le flux d'hydrocarbures légers comprenant de l'éthane et de l'éthylène ;
    (d) la mise en contact d'au moins une partie du flux d'hydrocarbures légers avec un adsorbeur d'hydrocarbures purgés pour produire un adsorbeur d'hydrocarbures chargés et un flux gazeux non adsorbé, au moins une partie d'éthane étant adsorbée par l'adsorbeur d'hydrocarbures purgés à une première pression pour donner de l'éthane adsorbé, et le flux gazeux non adsorbé comprenant de l'éthylène récupéré, l'éthylène récupéré comprenant au moins une partie de l'éthylène du flux d'hydrocarbures légers, l'adsorbeur d'hydrocarbures comprenant une structure d'imidazolate zéolithique (ZIF) ;
    (e) la mise en contact d'au moins une partie de l'adsorbeur d'hydrocarbures chargés avec un flux gazeux de balayage à une seconde pression pour produire un adsorbeur d'hydrocarbures déchargés et un flux gazeux adsorbé récupéré, le flux gazeux adsorbé récupéré comprenant au moins une partie du flux gazeux de balayage et au moins une partie d'éthane désorbé, l'éthane désorbé comprenant au moins une partie de l'éthane adsorbé, et la première pression étant supérieure à la seconde pression égale ou supérieure à environ 400 kPa ; et
    (f) la mise en contact d'au moins une partie de l'adsorbeur d'hydrocarbures déchargés avec au moins une partie du flux gazeux de balayage à la première pression pour donner l'adsorbeur d'hydrocarbures purgés et un gaz de balayage épuisé.
  15. Procédé selon la revendication 14, au moins une partie du flux gazeux de balayage et/ou au moins une partie du gaz de balayage épuisé étant mise en contact avec au moins une partie du flux d'hydrocarbures légers pendant (d) la mise en contact avec l'adsorbeur d'hydrocarbures purgés ;
    au moins une partie du flux gazeux non adsorbé étant séparée en un flux d'azote et un flux d'isobutane et d'éthylène ;
    au moins une partie du flux d'isobutane et d'éthylène étant recyclée comme réactif pour (a) polymériser l'éthylène ;
    au moins une partie du flux d'azote étant recyclée vers le flux gazeux de balayage ;
    au moins une partie du flux d'azote étant recyclée en un flux gazeux de purge en contact avec au moins une partie du flux étant de polymère ;
    au moins une partie du flux gazeux étant distillée en un flux de queue de distillation légère comprenant de l'isobutane sans oléfine, au moins une partie du flux de fond de distillation légère étant recyclée vers le flux gazeux de balayage ;
    au moins une partie du gaz de balayage épuisé étant recyclée vers le flux gazeux de balayage ; et
    au moins une partie du flux gazeux adsorbé récupéré étant recyclée vers un processus de production d'éthylène.
EP15861277.0A 2014-11-21 2015-11-19 Séparation d'éthylène à l'aide d'adsorption modulée en pression Active EP3207005B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US14/550,638 US9108891B1 (en) 2014-11-21 2014-11-21 Ethylene separation with pressure swing adsorption
PCT/US2015/061610 WO2016081738A1 (fr) 2014-11-21 2015-11-19 Séparation d'éthylène à l'aide d'adsorption modulée en pression

Publications (3)

Publication Number Publication Date
EP3207005A1 EP3207005A1 (fr) 2017-08-23
EP3207005A4 EP3207005A4 (fr) 2018-07-18
EP3207005B1 true EP3207005B1 (fr) 2021-06-16

Family

ID=53785904

Family Applications (1)

Application Number Title Priority Date Filing Date
EP15861277.0A Active EP3207005B1 (fr) 2014-11-21 2015-11-19 Séparation d'éthylène à l'aide d'adsorption modulée en pression

Country Status (8)

Country Link
US (3) US9108891B1 (fr)
EP (1) EP3207005B1 (fr)
CN (1) CN107108405A (fr)
BR (1) BR112017010465A2 (fr)
CA (1) CA2968047A1 (fr)
MX (1) MX2017006607A (fr)
RU (1) RU2017117511A (fr)
WO (1) WO2016081738A1 (fr)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9108891B1 (en) 2014-11-21 2015-08-18 Chevron Phillips Chemical Company Ethylene separation with pressure swing adsorption
CN105879575B (zh) * 2016-05-25 2019-02-26 中北大学 一种有害气体吸附实验装置
RU2750076C2 (ru) 2016-12-15 2021-06-21 ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи Сочетание мембранного способа и адсорбции с переменным давлением в установке получения изобутана и азота
CN107447231B (zh) * 2017-08-02 2019-02-22 中国石油大学(华东) 一种二碲化钴电催化析氧复合材料及其制备方法和应用
CN111655657B (zh) * 2017-12-05 2023-05-26 英力士美国化学公司 在具有变化的氢气吹扫压力的变压吸附装置中回收对二甲苯的方法
US10792609B2 (en) * 2018-05-07 2020-10-06 Chevron Phillips Chemical Company Lp Nitrogen conservation in polymerization processes
CN108962618A (zh) * 2018-07-17 2018-12-07 合肥工业大学 一种双壳层、蛋黄壳层氮掺杂空心多孔碳及其制备方法和应用
CN110237816B (zh) * 2019-06-13 2022-06-17 江苏科技大学 一种硝酸银修饰的金属有机骨架吸附材料的制备方法及其应用
CN112723976A (zh) * 2019-10-28 2021-04-30 中国石油化工股份有限公司 一种金属有机骨架材料回收炼厂干气用作乙烯原料的方法和系统
CN113209839B (zh) * 2021-05-11 2022-03-08 天津工业大学 一种具有高耐酸性能的甲烷/氮气分离的混合基质膜及制备方法和应用
CN114933917B (zh) * 2022-06-28 2023-08-22 福建清油夫实业有限公司 一种导热系统不停产清洗和导热油在线修复的方法

Family Cites Families (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3248179A (en) 1962-02-26 1966-04-26 Phillips Petroleum Co Method and apparatus for the production of solid polymers of olefins
US4501885A (en) 1981-10-14 1985-02-26 Phillips Petroleum Company Diluent and inert gas recovery from a polymerization process
US4588790A (en) 1982-03-24 1986-05-13 Union Carbide Corporation Method for fluidized bed polymerization
US5565175A (en) 1990-10-01 1996-10-15 Phillips Petroleum Company Apparatus and method for producing ethylene polymer
US5575979A (en) 1991-03-04 1996-11-19 Phillips Petroleum Company Process and apparatus for separating diluents from solid polymers utilizing a two-stage flash and a cyclone separator
US5352749A (en) 1992-03-19 1994-10-04 Exxon Chemical Patents, Inc. Process for polymerizing monomers in fluidized beds
US5436304A (en) 1992-03-19 1995-07-25 Exxon Chemical Patents Inc. Process for polymerizing monomers in fluidized beds
US5470925A (en) * 1993-09-30 1995-11-28 The Boc Group, Inc. Process for the production of alkene polymers
NZ264288A (en) * 1993-09-30 1996-08-27 Boc Group Inc Preparation of ethylene and propylene polymers from mixtures of ethylene/ethane and propylene/propane, respectively, with either pre-polymerisation or post-polmerisation adsorption of the unsaturated component and recycling of at least part of the unreacted monomer
US6239235B1 (en) 1997-07-15 2001-05-29 Phillips Petroleum Company High solids slurry polymerization
BE1011333A3 (fr) 1997-08-20 1999-07-06 Solvay Procede de fabrication d'une composition de polymeres d'ethylene.
ES2166632T3 (es) * 1998-03-18 2002-04-16 Boc Group Inc Procedimiento para la separacion de alquenos y alcanos.
KR100531628B1 (ko) 1998-03-20 2005-11-29 엑손모빌 케미칼 패턴츠 인코포레이티드 연속적인 슬러리 중합반응의 휘발물질 제거
US6262191B1 (en) 1999-03-09 2001-07-17 Phillips Petroleum Company Diluent slip stream to give catalyst wetting agent
EP1683834A3 (fr) 2001-03-01 2006-09-13 Borealis Technology Oy Compositions de polyéthylène utilisées dans le moulage par rotation
US7294599B2 (en) 2004-06-25 2007-11-13 Chevron Phillips Chemical Co. Acidic activator-supports and catalysts for olefin polymerization
US7163906B2 (en) 2004-11-04 2007-01-16 Chevron Phillips Chemical Company, Llp Organochromium/metallocene combination catalysts for producing bimodal resins
US7691771B2 (en) 2005-12-20 2010-04-06 Chevron U.S.A. Inc. Regeneration of ionic liquid catalyst by hydrogenation using a supported catalyst
US7732363B2 (en) 2005-12-20 2010-06-08 Chevron U.S.A. Inc. Regeneration of acidic catalysts
US7572944B2 (en) 2005-12-20 2009-08-11 Chevron U.S.A. Inc. Process for making and composition of superior lubricant or lubricant blendstock
US7572943B2 (en) 2005-12-20 2009-08-11 Chevron U.S.A. Inc. Alkylation of oligomers to make superior lubricant or fuel blendstock
US7576252B2 (en) 2005-12-20 2009-08-18 Chevron U.S.A. Inc. Process for the formation of a superior lubricant or fuel blendstock by ionic liquid oligomerization of olefins in the presence of isoparaffins
US7807597B2 (en) 2008-04-08 2010-10-05 Chevron U.S.A. Inc. Regeneration of ionic liquid catalyst using a regeneration metal in the presence of added hydrogen
US7619047B2 (en) 2006-02-22 2009-11-17 Chevron Phillips Chemical Company, Lp Dual metallocene catalysts for polymerization of bimodal polymers
KR20090004891A (ko) 2006-02-28 2009-01-12 더 리젠츠 오브 더 유니버시티 오브 캘리포니아 관능화된 제올라이트 골격들의 제조
US7732364B2 (en) 2007-12-28 2010-06-08 Chevron U.S.A. Inc. Process for ionic liquid catalyst regeneration
CA2618267C (fr) * 2008-01-21 2016-04-05 The Governors Of The University Of Alberta Zeolithes ets-10 pour la separation des olefines
US8142746B2 (en) * 2008-02-21 2012-03-27 Exxonmobil Research And Engineering Company Separation of carbon dioxide from methane utilizing zeolitic imidazolate framework materials
US8071063B2 (en) 2008-02-21 2011-12-06 Exxonmobile Research And Engineering Company Separation of hydrogen from hydrocarbons utilizing zeolitic imidazolate framework materials
US7955424B2 (en) 2008-10-30 2011-06-07 The Boeing Company System and method to make a fuel tank inert
US8101809B2 (en) 2009-08-10 2012-01-24 Chevron U.S.A. Inc. Base oil composition comprising oligomerized olefins
US8471086B2 (en) 2010-06-28 2013-06-25 Chevron U.S.A. Inc. Process to control product selectivity
US8524968B2 (en) 2010-12-13 2013-09-03 Chevron U.S.A. Inc. Process to make base oil by oligomerizing low boiling olefins
US8222471B2 (en) 2010-12-13 2012-07-17 Chevron U.S.A. Inc. Process for making a high viscosity base oil with an improved viscosity index
US8586812B2 (en) 2010-12-22 2013-11-19 Chevron U.S.A. Inc. Ionic liquid catalyzed olefin oligomerization for distillate production
EP2836284A2 (fr) * 2012-04-13 2015-02-18 Chevron Phillips Chemical Company LP Séparations de composants lors d'une polymérisation
WO2015031363A1 (fr) * 2013-08-30 2015-03-05 Exxonmobil Chemical Patents Inc. Stockage d'oxygène et production d'hydrocarbures en c5+
US9108891B1 (en) 2014-11-21 2015-08-18 Chevron Phillips Chemical Company Ethylene separation with pressure swing adsorption

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

Also Published As

Publication number Publication date
CA2968047A1 (fr) 2016-05-26
MX2017006607A (es) 2017-12-14
US20160144313A1 (en) 2016-05-26
EP3207005A1 (fr) 2017-08-23
RU2017117511A (ru) 2018-12-21
CN107108405A (zh) 2017-08-29
US9427694B2 (en) 2016-08-30
BR112017010465A2 (pt) 2018-04-03
EP3207005A4 (fr) 2018-07-18
US9227890B1 (en) 2016-01-05
WO2016081738A1 (fr) 2016-05-26
US9108891B1 (en) 2015-08-18

Similar Documents

Publication Publication Date Title
EP3207005B1 (fr) Séparation d'éthylène à l'aide d'adsorption modulée en pression
US9339755B2 (en) Ethylene separation with temperature swing adsorption
US11058987B2 (en) Membrane and pressure swing adsorption hybrid INRU process
EP2627679B1 (fr) Séparation améliorée de l'éthylène
RU2619690C2 (ru) Разделение компонентов при полимеризации
CN103459440B (zh) 用于加工反应器聚合流出物的系统和方法
US9187383B2 (en) Component separations in polymerization
EP2836285A1 (fr) Récupération d'éthylène par absorption
US20130312603A1 (en) Processes and sorbents for separation of gases by cyclic adsorption
CN1136235C (zh) 聚烯烃装置中分离烯烃的方法
EP3397654B1 (fr) Procédé amélioré de polymérisation d'oléfines en phase gazeuse fonctionnant en mode de condensation

Legal Events

Date Code Title Description
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE

PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20170518

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAV Request for validation of the european patent (deleted)
DAX Request for extension of the european patent (deleted)
A4 Supplementary search report drawn up and despatched

Effective date: 20180615

RIC1 Information provided on ipc code assigned before grant

Ipc: C07C 7/00 20060101AFI20180611BHEP

Ipc: C07C 7/04 20060101ALI20180611BHEP

Ipc: C08F 10/02 20060101ALI20180611BHEP

Ipc: C07C 7/13 20060101ALI20180611BHEP

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20190903

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20210209

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE PATENT HAS BEEN GRANTED

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 602015070533

Country of ref document: DE

REG Reference to a national code

Ref country code: AT

Ref legal event code: REF

Ref document number: 1402235

Country of ref document: AT

Kind code of ref document: T

Effective date: 20210715

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

REG Reference to a national code

Ref country code: NL

Ref legal event code: FP

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG9D

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210916

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210917

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

Ref country code: NO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210916

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

REG Reference to a national code

Ref country code: AT

Ref legal event code: UEP

Ref document number: 1402235

Country of ref document: AT

Kind code of ref document: T

Effective date: 20210616

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

Ref country code: SM

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20211018

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 602015070533

Country of ref document: DE

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

26N No opposition filed

Effective date: 20220317

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20211119

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211119

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211119

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211119

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HU

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO

Effective date: 20151119

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

P01 Opt-out of the competence of the unified patent court (upc) registered

Effective date: 20230526

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20220630

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20220630

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20231020

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20231019

Year of fee payment: 9

Ref country code: DE

Payment date: 20231019

Year of fee payment: 9

Ref country code: AT

Payment date: 20231023

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 20231019

Year of fee payment: 9

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: TR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210616